CN205216582U - Iron and steel sintering flue gas is synthesized desulfurization, denitration and is got rid of device of dioxin - Google Patents
Iron and steel sintering flue gas is synthesized desulfurization, denitration and is got rid of device of dioxin Download PDFInfo
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- CN205216582U CN205216582U CN201520890217.4U CN201520890217U CN205216582U CN 205216582 U CN205216582 U CN 205216582U CN 201520890217 U CN201520890217 U CN 201520890217U CN 205216582 U CN205216582 U CN 205216582U
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Abstract
The utility model provides a device, the device mainly includes: that iron and steel sintering flue gas desulfurization, denitration and get rid of the dioxin GGH heat exchanger, flue gas heating furnace, ammonia injection grid, SCR reactor, flue gas - water heat exchanger, booster fan, circulating water pump, desulfurizing tower, chimney etc, desulfurated technology after the first denitration of this method adoption: sintering flue gas after the dust removal inserts the SCR flue gas denitration device earlier behind main air exhauster, get rid of NOX and dioxin, and then the desulfurization of wet flue gas desulfurization tower gets into, the sintering flue gas is after chimney discharge to reach standard. The utility model discloses an aspect enables sintering flue gas discharge to reach standard, eliminates the chimney and emits " white cigarette " phenomenon, reduces flue gas heating power consumption simultaneously, the energy saving.
Description
Technical field
The utility model belongs to steel sintering production environment protection field, is specifically related to a kind of SO comprehensively removed in steel sintering flue gas
2, NO
xthe device of Ji bioxin.
Background technology
SINTERING PRODUCTION is that modern steel produces one of most important technique unit, is also the heavy polluter of steel and iron industry simultaneously.Sintering circuit NO
xdischarge capacity accounts for 50%, S0 of steel and iron industry total release
2discharge capacity accounts for 60% of steel and iron industry total release, and steel industry sintering and electric furnace produce bioxin and account for 25.9% of national dioxin emission total amount.Along with the raising day by day that Environmental Protection in China requires, not only to sinter fume dust and SO
2discharge is more strict, simultaneously to NO
xthe discharge of He bioxin it is also proposed new requirement.
In recent years, China's sinter fume SO
2improvement receive remarkable effect, the techniques such as such as wet method (limestone-gypsum method, magnesium processes, ammonia process etc.), ciculation fluidized bed process (CFB), rotary spraying technique (SDA) all have engineer applied, and technology maturation, stable performance.
But China is for sinter fume NO
xthe improvement of He bioxin is just at the early-stage, and current China sinter fume synthesis desulfurating, denitration and the technology removing bioxin are: the technique adopting wet desulphurization+SCR denitration and remove bioxin is to process sinter fume.Its flow process is, denitration after first desulfurization: sinter fume (130 DEG C) is sent into desulfurizing tower by main exhauster and removed SO after dedusting
2, the flue-gas temperature after desulfurization is down to 50 DEG C ~ 60 DEG C, and then deliver to SCR reactor carry out denitration and remove bioxin; Because reaction temperature in SCR reactor is between 320 DEG C ~ 400 DEG C, so need to arrange GGH heat exchanger and fume heating furnace, flue-gas temperature is promoted to more than 320 DEG C, just can enters SCR reactor reaction.Sinter fume through wet desulphurization+SCR denitration with after removing bioxin device, its SO
2, NO
xhe bioxin all can qualified discharge.
Prior art weak point mainly energy consumption is large.Wet desulphurization+SCR denitration and removal bioxin technology, need 50 DEG C ~ 60 DEG C desulfurization wet flue gas be heated to more than the 320 DEG C effective denitrations of ability and remove bioxin, fuel consumption is many.
Utility model content
For prior art Problems existing, the purpose of this utility model is to provide a kind of less energy consumption, the steel sintering smoke comprehensive desulphurization and denitration that can reduce operating cost and the device and method removing bioxin.It can make sinter fume qualified discharge, eliminates chimney and emits " white cigarette " phenomenon, reduce system drag overall and flue gas energy consumption, economize energy.
According to first embodiment of the present utility model, the desulfurization of a kind of steel sintering smoke comprehensive is provided, the device of denitration and removal bioxin, this device comprises: according to flow of flue gas direction, main exhauster (1), along with flue gas flow direction, also comprise the first heat transfer zone (201) being arranged on the top-right GGH heat exchanger (2) of main exhauster (1), be arranged on the fume heating furnace (3) in the first heat transfer zone (201) downstream of GGH heat exchanger (2) top, be arranged on the ammonia-spraying grid (4) above fume heating furnace (3) downstream, be arranged on the SCR reactor (5) of ammonia-spraying grid (4) right, downstream, be positioned at second heat transfer zone (202) of the GGH heat exchanger (2) in SCR reactor (5) downstream, be positioned at below and with first heat transfer zone (601) of the gas-water heat exchanger (6) be connected within second heat transfer zone (202) of GGH heat exchanger (2), be positioned at the booster fan (7) of the cigarette airflow downstream of first heat transfer zone (601) of gas-water heat exchanger (6), be positioned at the desulfurizing tower (8) (preferably wet desulfuration tower) of booster fan (7) right, downstream, and be positioned at second heat transfer zone (602) of gas-water heat exchanger (6) at desulfurizing tower (8) top, and be positioned at the downstream of the second heat transfer zone (602) or the chimney (9) at top of gas-water heat exchanger (6).
Preferably, desulfurizing tower (8) (preferably wet desulfuration tower) has tower height (referring to main body tower height) and/or the 2-20 rice of 2-25 rice, preferably 3-20 rice, more preferably 4-16 rice, more preferably 5-12 rice
2, more preferably 3-16 rice
2, more preferably 4-10 rice
2inside (i.e. tower wall surround internal chamber) cross-sectional area.
Preferably, said apparatus also comprises the water circulating pump (10) be positioned between first heat transfer zone (601) of gas-water heat exchanger (6) and the second heat transfer zone (602) chimney (9) of gas-water heat exchanger (6).
Preferably, between first heat transfer zone (601) and the second heat transfer zone (602) of gas-water heat exchanger (6), have the peripheral passage of the water as heat exchange medium, wherein water circulating pump (10) is positioned among this peripheral passage.
Preferably, fume heating furnace (3) uses coal gas or natural gas as fuel, for adding the heating furnace of heat smoke.
Preferably, in SCR reactor (5), TiO is housed
2/ V
2o
5/ WO
3catalyst.
According to second embodiment of the present utility model, provide a kind of and use the steel sintering smoke comprehensive desulphurization and denitration of said apparatus and remove the method for bioxin, the method mainly comprises:
1) the former flue gas of the sintering after dedusting via main exhauster (1) be delivered in first heat transfer zone (201) of GGH heat exchanger (2) with the denitration of discharging from SCR reactor (5) after flue gas carry out indirect heat exchange and heat up;
2) enter further heat temperature raising fume heating furnace (3) from the flue gas after the intensification that first heat transfer zone (201) of GGH heat exchanger (2) is discharged and become high-temperature flue gas;
3) above step 2) high-temperature flue gas then flow through ammonia-spraying grid (4) and be injected into ammonia and become the high-temperature flue gas carrying ammonia;
4) high-temperature flue gas carrying ammonia enters into the SCR reactor (5) being mounted with Selective catalytic reduction catalyst and carries out Selective catalytic reduction denitration reaction, obtains flue gas after denitration;
5) twice heat exchange of flue gas after denitration: after the denitration of discharging from SCR reactor (5) flue gas be transported in GGH heat exchanger (2) with the dedusting in first heat transfer zone (201) of input GGH heat exchanger (2) after the former flue gas of sintering carry out indirect heat exchange and experience first time heat exchange and lower the temperature; Enter into first heat transfer zone (601) of the gas-water heat exchanger (6) of the second heat transfer zone (202) being arranged in GGH heat exchanger (2) subsequently and carry out indirect heat exchange as the water [it circulates between first heat transfer zone (601) and the second heat transfer zone (602) of gas-water heat exchanger (6)] of heat exchange medium and experience second time heat exchange and lower the temperature;
6) the cooling flue gas of discharging 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) water [it circulates between first heat transfer zone (601) and the second heat transfer zone (602) of gas-water heat exchanger (6)] that the flue gas after desulfurization flows through subsequently in second heat transfer zone (602) of gas-water heat exchanger (6) and as heat exchange medium carries out indirect heat exchange and again heats up, and becomes the flue gas again heated up; With
8) flue gas again heated up is discharged, such as, discharge via chimney (9).
Generally, in step 1) in be warming up to 280 DEG C ~ 320 DEG C by indirect heat exchange.
Generally, 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 experience second time heat exchange after denitration and be cooled to 100 DEG C ~ 140 DEG C, preferably 110 DEG C ~ 130 DEG C.
Preferably, the neat stress temperature in the desulfurizing tower (8) after desulfurization 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 again warming up to 90-120 DEG C, more preferably 100-110 DEG C.
In the above-mentioned methods, in SCR reactor (5), TiO is housed
2/ V
2o
5/ WO
3catalyst.
Briefly, a kind of steel sintering smoke comprehensive of the present utility model desulfurization, the device of denitration and removal bioxin comprises: main exhauster, along with flue gas flow direction, also comprise and be arranged on the top-right GGH heat exchanger of main exhauster (namely, gas-to-gas heat exchanger, gas-gasheater), be arranged on the fume heating furnace above GGH heat exchanger, be arranged on the ammonia-spraying grid above fume heating furnace, be arranged on the SCR reactor of ammonia-spraying grid right (namely, Selective catalytic reduction (denitration) reactor), be positioned at the gas-water heat exchanger be connected below SCR reactor and with GGH heat exchanger, be positioned at the booster fan of the cigarette airflow downstream of gas-water heat exchanger, be positioned at the desulfurizing tower of booster fan right and be positioned at the chimney at desulfurizing tower top.
In addition, said apparatus also comprises the water circulating pump between gas-water heat exchanger and chimney.
The utility model also provides a kind of steel sintering smoke comprehensive desulphurization and denitration and removes the method for bioxin or a kind of steel sintering smoke comprehensive desulphurization and denitration using said apparatus and the method removing bioxin, the method mainly comprises: the former flue gas of the sintering after dedusting first accesses SCR equipment for denitrifying flue gas after main exhauster, and then enter wet desulfuration tower, finally by chimney qualified discharge.
In the process preferably, the former flue gas of sintering after dedusting (as 130 DEG C) is before main exhauster enters SCR reactor, be introduced into GGH heat exchanger and be heated to 280 DEG C ~ 320 DEG C, then enter fume heating furnace to continue to be heated to 320 DEG C ~ 350 DEG C, then send into SCR reactor after ammonia-spraying grid ammonification.
Preferably, add pyrogen flue gas from SCR reactor neat stress (320 DEG C ~ 350 DEG C) out by GGH heat exchanger, make former flue-gas temperature rise to 280 DEG C ~ 320 DEG C, the neat stress temperature after heat exchange is down to 160 DEG C ~ 180 DEG C.
Preferably, gas-water heat exchanger is entered from GGH heat exchanger neat stress (160 DEG C ~ 180 DEG C) out, neat stress temperature after heat exchange is down to about 120 DEG C, and then neat stress delivers to desulfurizing tower desulfurization with booster fan, and the neat stress temperature after desulfurization is at 50 DEG C ~ 60 DEG C.
Preferably, the heat delivery contained in the neat stress (160 DEG C ~ 180 DEG C) that gas-water heat exchanger adopts water circulating pump to be discharged by GGH heat exchanger is to desulfurizing tower exit, heating desulfurizing tower exiting flue gas, make the flue gas after desulfurization be warming up to about 100 DEG C, the clean flue gas after denitration, removal bioxin and desulfurization is by desulfurizing tower top chimney qualified discharge.
In this application, GGH heat exchanger is heat pipe-type GGH heat exchanger or swinging GGH heat exchanger.
In the method for the application, the flow flowing through the sinter fume of the utility model device is 100000Nm
3/ h-1400000Nm
3/ h is (as 400000Nm
3/ h, 700000Nm
3/ h, 900000Nm
3/ h).Entering the flue-gas temperature before this device is 120 DEG C-150 DEG C (as 130 DEG C).Flue gas SO
2concentration is generally 1000mg/Nm
3-2000mg/Nm
3(as 1500mg/Nm
3).NO in flue gas
xconcentration is generally 200mg/Nm
3-600mg/Nm
3(as 400mg/Nm
3).Adopt wet desulphurization, flue gas after desulfurization temperature is generally 55 DEG C-65 DEG C (as 60 DEG C), and desulfuration efficiency is more than 90% or 95%.Adopt SCR denitration, denitration reaction temperature is generally 280 DEG C-420 DEG C (as 350 DEG C or 360 DEG C), denitration efficiency more than 80%.
The beneficial effects of the utility model:
1, the flue-gas temperature of the utility model required for denitration desulfurization, before SCR reactor is arranged in sintering flue gas desulfurization tower, flue-gas temperature is only needed to be heated to more than 320 DEG C from 130 DEG C, and prior art needs flue-gas temperature to be heated to more than 320 DEG C from 50 DEG C ~ 60 DEG C, thus the utility model reduces a large amount of fuel consumption;
2, the utility model exports at GGH heat exchanger neat stress, gas-water heat exchanger is set before flue gas booster fan, reduce the flue gas volume flow entering booster fan on the one hand, decrease booster fan power consumption, improve desulfurizing tower exit gas temperature on the other hand, effectively can alleviate smoke evacuation sour corrosion and eliminate chimney and emit " white cigarette " phenomenon.
3, the temperature rise in each heat exchange link and the amplitude of temperature drop match each other, and overall heating efficiency is high.
Accompanying drawing explanation
Fig. 1: steel sintering flue gas desulfurization, denitration and removal bioxin process chart.
Reference numeral:
1: main exhauster; 2:GGH heat exchanger; First heat transfer zone of 201:GGH heat exchanger; The smoke inlet of the first heat transfer zone of 20101:GGH heat exchanger; The exhanst gas outlet of the first heat transfer zone of 20102:GGH heat exchanger; Second heat transfer zone of 202:GGH heat exchanger; The smoke inlet of the second heat transfer zone of 20201:GGH heat exchanger; The exhanst gas outlet of the second heat transfer zone of 20202:GGH heat exchanger; 3: fume heating furnace; 301: the smoke inlet of fume heating furnace; 302: the exhanst gas outlet of fume heating furnace; 4: ammonia-spraying grid; 5:SCR reactor; The smoke inlet of 501:SCR reactor; The exhanst gas outlet of 502:SCR reactor; 6: gas-water heat exchanger; 601: the first heat transfer zone of gas-water heat exchanger; 602: the second heat transfer zone of gas-water heat exchanger; 7: booster fan; 8: desulfurizing tower: 9: chimney; 10: water circulating pump.
Detailed description of the invention
In detailed description of the invention below, adopt the desulfurization of a kind of steel sintering smoke comprehensive, the device of denitration and removal bioxin, shown in Figure 1, this device comprises: main exhauster 1, along with flue gas flow direction, also comprise and be arranged on the top-right GGH heat exchanger 2 of main exhauster 1, be arranged on the fume heating furnace 3 above GGH heat exchanger 2, be arranged on the ammonia-spraying grid 4 above fume heating furnace 3, be arranged on the SCR reactor 5 of ammonia-spraying grid 4 right, be positioned at the gas-water heat exchanger 6 be connected below SCR reactor 5 and with GGH heat exchanger 2, be positioned at the booster fan 7 of the cigarette airflow downstream of gas-water heat exchanger 6, be positioned at the desulfurizing tower 8 of booster fan 7 right and be positioned at the chimney 9 at desulfurizing tower 8 top.
In addition, said apparatus also comprises the water circulating pump 10 between gas-water heat exchanger 6 and chimney 9.
In addition, adopt a kind of steel sintering smoke comprehensive desulphurization and denitration using the above device and the method removing bioxin, the method mainly comprises: the former flue gas of the sintering after dedusting, SCR equipment for denitrifying flue gas 5 is first accessed after main exhauster 1, and then enter wet desulfuration tower 8, discharge finally by chimney 9.
Preferably, the former flue gas of sintering after dedusting (as 130 DEG C) is before main exhauster 1 enters SCR reactor 5, be introduced into GGH heat exchanger 2 and be heated to 280 DEG C ~ 320 DEG C, then enter fume heating furnace 3 to continue to be heated to 320 DEG C ~ 350 DEG C, then send into SCR reactor 5 after ammonia-spraying grid 4 ammonification.
Preferably, add pyrogen flue gas from SCR reactor 5 neat stress (320 DEG C ~ 350 DEG C) out by GGH heat exchanger 2, make former flue-gas temperature rise to 280 DEG C ~ 320 DEG C, the neat stress temperature after heat exchange is down to 160 DEG C ~ 180 DEG C.
Preferably, gas-water heat exchanger 6 is entered from GGH heat exchanger 2 neat stress (160 DEG C ~ 180 DEG C) out, neat stress temperature after heat exchange is down to about 120 DEG C, and then neat stress delivers to desulfurizing tower 8 desulfurization with booster fan 7, and the neat stress temperature after desulfurization is at 50 DEG C ~ 60 DEG C.
Preferably, the heat delivery contained in the neat stress (160 DEG C ~ 180 DEG C) that gas-water heat exchanger 6 adopts water circulating pump 10 to be discharged by GGH heat exchanger 2 is to desulfurizing tower 8 exit, heating desulfurizing tower 8 exiting flue gas, make the flue gas after desulfurization be warming up to about 100 DEG C, the clean flue gas after denitration, removal bioxin and desulfurization is by desulfurizing tower 8 top chimney 9 qualified discharge.
GGH heat exchanger 2 is heat pipe-type GGH heat exchanger or swinging GGH heat exchanger.
Embodiment
Certain 180m
2sintering machine, sinter fume amount is 700000Nm
3/ h, flue-gas temperature is 130 DEG C, flue gas SO
2concentration is 1500mg/Nm
3, flue gas NO
xconcentration is 400mg/Nm
3.Adopt wet desulphurization, flue gas after desulfurization temperature 60 C, desulfuration efficiency 90%; Adopt SCR denitration, denitration reaction temperature 350 DEG C, denitration efficiency 80%.Flue gas adopts coke-stove gas, and coke-stove gas calorific value is 16720kJ/Nm
3(4000kcal/Nm
3).
The utility model compares with coke-stove gas consumption in prior art (denitration after first desulfurization):
A. Fuel Consumption of the present utility model:
The utility model adopts the technique of desulfurization after first denitration: the former flue gas of the sintering after dedusting (130 DEG C), after main exhauster, enter GGH heat exchanger (heat pipe-type GGH heat exchanger) be heated to 310 DEG C, then fume heating furnace is entered, continue to be heated to 350 DEG C, SCR reactor is sent into again, by catalyst removal NO in SCR reactor after ammonia-spraying grid ammonification
xand bioxin, add pyrogen flue gas from SCR reactor neat stress (350 DEG C) out by GGH heat exchanger, make former flue gas be warming up to 310 DEG C, the neat stress temperature after heat exchange is down to 170 DEG C.In whole process, GGH heat exchanger thermal source is the neat stress waste heat after SCR reactor, and the fuel consumed is only needed for fume heating furnace.
Former flue gas is heated to 350 DEG C of fuel quantity E1 consumed by 310 DEG C by fume heating furnace:
E1＝(V×I
y2-V×I
y1)/Q/η(1)
＝(700000×479.5-700000×423.5)/16720/0.85
＝2758Nm
3/h
V---flue gas volume 700000Nm
3/ h
I
y2---flue gas enthalpy 479.5kJ/Nm when 350 DEG C
3(tabling look-up)
I
y1---flue gas enthalpy 423.5kJ/Nm when 310 DEG C
3(tabling look-up)
Q---coke-stove gas calorific value 16720kJ/Nm
3(4000kcal/Nm
3)
η---fume heating furnace heat utilization efficiency, gets 0.85
B. the Fuel Consumption of prior art (denitration after first desulfurization):
Denitration after prior art desulfurization: sinter fume (130 DEG C) is sent into desulfurizing tower by main exhauster and removed SO after dedusting
2, the flue-gas temperature after desulfurization is down to 60 DEG C, then enters GGH heat exchanger and is warming up to 280 DEG C, then enter fume heating furnace, continues to be heated to 350 DEG C, then send into SCR reactor after ammonia-spraying grid ammonification, by catalyst removal NO in SCR reactor
xand bioxin, add the flue gas after thermally desulfurizing from SCR reactor neat stress (350 DEG C) out by GGH heat exchanger, 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 reactor, and the fuel consumed is needed for fume heating furnace.
Former flue gas is heated to 350 DEG C of fuel quantities consumed by 280 DEG C by fume heating furnace:
E2＝(V×Iy2-V×Iy1)/Q/η(2)
＝(700000×479.5-700000×381.5)/16720/0.85
＝4827Nm
3/h
Iy2---flue gas enthalpy 479.5kJ/Nm when 350 DEG C
3(tabling look-up)
Iy1---flue gas enthalpy 381.5kJ/Nm when 280 DEG C
3(tabling look-up)
In formula (2), all the other alphabetical symbolic significances are identical with formula (1).
The utility model saves coke-stove gas percentage than prior art:
γ＝(E2-E1)/E2×100％(3)
＝(4827-2758)/4827×100％
＝42.86％
The utility model saves 42.86% than prior art (denitration after first desulfurization) coke-stove gas consumption.
Claims (8)
1. steel sintering smoke comprehensive desulfurization, the device of denitration and removal bioxin, this device comprises: according to flow of flue gas direction, main exhauster (1), first heat transfer zone (201) of GGH heat exchanger (2), be arranged on the fume heating furnace (3) in the first heat transfer zone (201) downstream of GGH heat exchanger (2), be arranged on the ammonia-spraying grid (4) in fume heating furnace (3) downstream, be arranged on the SCR reactor (5) in ammonia-spraying grid (4) downstream, be positioned at second heat transfer zone (202) of the GGH heat exchanger (2) in SCR reactor (5) downstream, first heat transfer zone (601) of the gas-water heat exchanger (6) within the second heat transfer zone (202) being positioned at GGH heat exchanger (2), be positioned at the booster fan (7) of the cigarette airflow downstream of first heat transfer zone (601) of gas-water heat exchanger (6), be positioned at the desulfurizing tower (8) in booster fan (7) downstream, be positioned at second heat transfer zone (602) of the gas-water heat exchanger (6) at desulfurizing tower (8) top, and be positioned at the downstream of the second heat transfer zone (602) or the chimney (9) at top of gas-water heat exchanger (6),
Wherein desulfurizing tower (8) has tower height and/or the 2-20m of 2-25 rice
2internal cross-sectional area.
2. device according to claim 1, is characterized in that: it also comprises the water circulating pump (10) be positioned 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 characterized in that: the peripheral passage between first heat transfer zone (601) and the second heat transfer zone (602) of gas-water heat exchanger (6) with the water as heat exchange medium, wherein water circulating pump (10) is positioned among this peripheral passage.
4. device according to claim 1 and 2, is characterized in that fume heating furnace (3) uses coal gas or natural gas as fuel, for adding the heating furnace of heat smoke.
5. device according to claim 3, is characterized in that fume heating furnace (3) uses coal gas or natural gas as fuel, for adding the heating furnace of heat smoke.
6. device according to claim 1 and 2, is characterized in that, in SCR reactor (5), TiO is housed
2/ V
2o
5/ WO
3catalyst.
7. device according to claim 3, is characterized in that, in SCR reactor (5), TiO is housed
2/ V
2o
5/ WO
3catalyst.
8. device according to claim 4, is characterized in that, in SCR reactor (5), TiO is housed
2/ V
2o
5/ WO
3catalyst.
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|---|---|---|---|
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ID=55891678
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| CN105944565A (en) * | 2016-06-16 | 2016-09-21 | 北京方信立华科技有限公司 | Integrated energy-saving SCR denitration device |
| CN106925078A (en) * | 2017-03-15 | 2017-07-07 | 上海交通大学 | A kind of ultra-clean reheating exhaust system of desulfurization and the method based on the system |
| CN108686504A (en) * | 2017-04-05 | 2018-10-23 | 辽宁中弘信冶金技术有限公司 | The processing system and method for flue gases of cock oven |
| CN109432936A (en) * | 2018-12-04 | 2019-03-08 | 中冶南方都市环保工程技术股份有限公司 | Sintering flue gas processing method and processing system |
| CN113398757A (en) * | 2021-06-24 | 2021-09-17 | 南方电网电力科技股份有限公司 | Simple ammonia injection control method and device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105944565A (en) * | 2016-06-16 | 2016-09-21 | 北京方信立华科技有限公司 | Integrated energy-saving SCR denitration device |
| CN105944565B (en) * | 2016-06-16 | 2019-09-03 | 北京方信立华科技有限公司 | Integrated energy-saving SCR denitration device |
| CN106925078A (en) * | 2017-03-15 | 2017-07-07 | 上海交通大学 | A kind of ultra-clean reheating exhaust system of desulfurization and the method based on the system |
| CN108686504A (en) * | 2017-04-05 | 2018-10-23 | 辽宁中弘信冶金技术有限公司 | The processing system and method for flue gases of cock oven |
| CN109432936A (en) * | 2018-12-04 | 2019-03-08 | 中冶南方都市环保工程技术股份有限公司 | Sintering flue gas processing method and processing system |
| CN113398757A (en) * | 2021-06-24 | 2021-09-17 | 南方电网电力科技股份有限公司 | Simple ammonia injection control method and device |
| CN113398757B (en) * | 2021-06-24 | 2022-05-17 | 南方电网电力科技股份有限公司 | Simple ammonia injection control method and device |
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