CN1986031A - Process and apparatus for eliminating fume SO2 from waste coking ammonia water of iron and steel and coal chemical enterprise - Google Patents

Process and apparatus for eliminating fume SO2 from waste coking ammonia water of iron and steel and coal chemical enterprise Download PDF

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Publication number
CN1986031A
CN1986031A CN 200610048701 CN200610048701A CN1986031A CN 1986031 A CN1986031 A CN 1986031A CN 200610048701 CN200610048701 CN 200610048701 CN 200610048701 A CN200610048701 A CN 200610048701A CN 1986031 A CN1986031 A CN 1986031A
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absorption
mother liquor
tower
flue gas
pump
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CN 200610048701
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CN100430113C (en
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曾子平
刘应隆
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云南亚太环境工程设计研究有限公司
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Abstract

The present invention belongs to the field of chemical industry and environment protection technology, and is especially process and apparatus for eliminating SO2 from fume with waste coking ammonia water in iron and steel and coal chemical enterprise. The process of eliminating SO2 from fume uses low concentration ammonia water from coking production as the ammonia source of the absorbent and has Fe+3 or S2O3-2 ion added in the oxidation process before ammonium sulfate is recovered. The apparatus consists of a high-level ammonia water tank, an absorption column, an absorbing liquid circulating pump, a catalyst solution tank, an absorbing liquid conveying pump, a blower, a fume cooling and mother liquid concentrating tower, a salt oxidizing tower, an ammonium sulfate mother liquid circulating tank, a star valve, an ammonium sulfate output filtering pump, a filter and an ammonium sulfate circulating pump.

Description

Iron and steel, coal chemical enterprise waste coking ammonia water remove flue gas SO 2Technology and device
Technical field:
The present invention relates to a kind of iron and steel, the coal chemical enterprise waste coking ammonia water removes flue gas SO 2Technology and device, belong to Chemical Engineering and environmental protection technical field.
Relate to iron and steel, coal chemical enterprise utilizes the self-produced low concentration deposed ammonia of coking device to remove steel sintering flue gas or boiler smoke SO 2, reach curb environmental pollution, the purpose of comprehensive utilization of resources production fertilizer product.
Background technology:
Ammonia process absorbs SO 2Be to utilize the classical principles of chemistry, a kind of is the directly SO in spray and the flue gas of ammoniacal liquor 2Directly generate (NH 4) 2SO 3, NH 4HSO 3, this direct method ammonia loss is big, secondary pollution is big, cost is high.Industrial application desulfurization is to utilize (NH 4) 2SO 3Absorb SO 2Form NH 4HSO 3, the ammonia that replenishes makes NH 4HSO 3Be converted into (NH again 4) 2SO 3, realize
Little, the stable absorption of circulation ammonia consumption.Utilize the low concentration SO in the ammonia process reclaim sulfuric acid production tail gas 2, make the flue gas qualified discharge, can obtain (NH after the absorption 4) 2SO 3, NH 4HSO 3, use ammonia-acid system in general sulfuric acid plant, the mother liquor after the absorption adds excessive H 2SO 4Decompose inferior salt, decompose the SO that separates the sucking-off suitable concentration in the inferior salt process 2Return relieving haperacidity, stripping liquid is through NH 3Obtain (NH after the neutralization 3) 2SO 4Solution obtains product after evaporation, crystallization, drying.Conventional art is applicable to exhaust gas volumn and SO 2The desulfurization of concentration stabilize situation, utilize outsourcing liquefied ammonia or carbonic acid ammonia to do the ammonia source, the liquefied ammonia gasification is dissolved in water formation ammoniacal liquor and directly adds absorption mother liquor as initial absorption agent adding absorption mother liquor or gas ammonia, the method of utilizing liquefied ammonia to do the raw material ammonification need be provided with the ammonia station of press device, invest bigger, and ammonia evaporation power consumption.Then cost is higher to utilize carbon ammonia, and the large desulfurization device does not generally adopt.
Enterprise's flue gas desulfurization for no sulfuric acid production plant need be built sulfuric acid apparatus with said method, and investment is big, all absorbs SO at the exploitation ammonia process both at home and abroad at present 2The method that the inferior salt direct oxidation that forms is an ammonium sulfate.
The present invention has obtained Patent right " low concentration SO 2Directly prepare K after the smoke absorption oxidation 2SO 4Method and device thereof " a kind of SO of flue gas preferably disclosed 2Removal methods.
Summary of the invention:
The present invention is directed to enterprise's flue gas desulfurization of coking plant, directly utilize the ammonia source of the low concentration deposed ammonia of coking production as absorbent, the ammonia of coking is reclaimed link with flue gas desulfurization technique, minimizing coking ammonia still process energy consumption does not need to build the ammonia station, realization flue gas SO 2And the technology of charking deposed ammonia recycling, reach and curb environmental pollution, obtain the purpose of chemical fertilizer simultaneously.
The present invention improves to form on the basis of traditional ammonia process absorption and inferior salt oxidation technology.This technology is improved prior art.This technology directly utilizes the low concentration deposed ammonia of 2%-20% of coking production as the ammonia source of absorbent, is used for sinter fume or fire coal boiler fume SO 2Remove; In the inferior salt oxidizing process of two-stage oxidation, add Fe + 3Or S 2O 3 -2, handle back flue gas qualified discharge, the reclaim sulfuric acid ammonium; Detailed process is as follows:
A.130-150 ℃ hot flue gas or boiler smoke from iron and steel or coal chemical enterprise sintering enter with the reverse jet tube top of 20-27m/s gas speed from flue gas cooling and mother liquor concentration tower (7) top, and the reverse jet tube bottom upwards sprays into 50 ℃, density 1200-1230g/cm by nozzle 3The sulphur ammonium salt solution, liquid gas volume ratio L/G is 3/1000, after thermal insulation is cooled to 50-65 ℃ in the contrary spray of this turbulent flow tower, flue gas is from the flue gas cooling and discharge at mother liquor concentration tower (7) top and (2) top reverse jet tube enters from the absorption tower with 20-27m/s gas speed, form the foam absorption with total salt concentration 250-350g/L, basicity 5-15tt ° absorption mother liquor adverse current, volume ratio L/G=5/1000~7/1000, absorptivity>95%, gas SO 2Qualified discharge;
B. bottom, absorption tower (2) is the absorption mother liquor circulating slot, and the coking ammonia water of 2%-20% is directly mended in the Recycling Mother Solution groove of bottom, absorption tower (2), 5-15tt ° of absorption liquid basicity, pH value 5.5-6.2, density 1130-1150g/cm 3By absorption liquid circulating pump (3) circulation absorption mother liquor, absorption liquid delivery pump (5) is squeezed into nitrite oxidation column (8) with the absorption tower mother liquor of discharging, and blasts air by air blast (6) to nitrite oxidation column (8) simultaneously and carries out oxidation, and the amount that blasts air is by tower section 60-100m 3/ m 2.h calculate, inferior salt oxygenation efficiency>98%, residual gas imports flue gas cooling and mother liquor concentration tower (7) through the bubble-cap blast cap; Ammonium sulfate liquor circulating slot (9) is gone in the oxidation mother liquor overflow, by ammonium sulfate circulating pump (13) by volume L/G=3/1000 carry mother liquor to flue gas cooling and mother liquor concentration tower (7) reverse jet tube lower end from shower nozzle to the reverse spray of gas, the gas thermal insulation is cooled to 50-65 ℃, mother liquor is concentrated into 400-500g/L, it is 6 o'clock that the thickener mother liquor adds ammoniacal liquor adjusting PH, deliver to filter (12) with sulphur ammonium liquid output filtering pump (11) and filter, again through evaporation, concentrate, behind the crystallizing and drying product;
C. catalyst Fe + 3Or S 2O 3 -2Adding: the catalyst addition replenishes by the 0.01-0.03mol/L of absorption mother liquor discharge rate hourly, be made into 20% aqueous solution, respectively absorption liquid circulating pump (3) and absorption liquid delivery pump (5) import department intermittently mend into, wherein: 1/3 of the aqueous solution mends absorption liquid circulating pump (3) inlet, and 2/3 of the aqueous solution mends absorption liquid delivery pump (5) inlet.
It is this technological design home-built equipment that this method adopts equipment absorption tower (2) in the device, flue gas cooling and mother liquor concentration tower (7), nitrite oxidation column (8), and all the other are bought for market.This device is by ammoniacal liquor head tank (1), the absorption tower (2) that is connected with ammoniacal liquor head tank (1) by pipeline, place the absorption liquid circulating pump (3) and the absorption liquid delivery pump (5) of bottom, absorption tower (2) respectively, the catalyst solution groove (4) that is connected with the carrier pipe of absorption liquid circulating pump (3) and absorption liquid delivery pump (5) respectively, the nitrite oxidation column (8) that is connected with absorption liquid delivery pump (5) by pipeline and absorption tower (2), place the air blast (6) of nitrite oxidation column (8) bottom, by the cooling of pipeline and flue gas and mother liquor concentration tower (7) is connected and the bottom is provided with the ammonium sulfate liquor circulating slot (9) of star valve (10), the sulphur ammonium liquid output filtering pump (11) that is connected with star valve (10), the filter (12) that is connected with sulphur ammonium liquid output filtering pump (11), form with the ammonium sulfate circulating pump (13) that flue gas cooling and mother liquor concentration tower (7) are connected with ammonium sulfate liquor circulating slot (9) respectively by pipeline.
The present invention compared with prior art has the deposed ammonia that directly utilizes 2%-20%, is used for sinter fume or fire coal boiler fume SO 2Remove, that saves press device sets up the construction of ammonia station, has reduced the energy consumption of coking condensation ammoniacal liquor ammonia still process simultaneously, has reduced the treating capacity of coking ammonia-containing water, thereby has improved the economic benefit of coking; Simultaneously, reduced the production cost of desulfurization and sulphur ammonium, dust removing effects significantly improves, and makes flue gas desulfurization produce ammonium sulfate and has advantages such as favorable economic benefit.
Description of drawings:
Accompanying drawing is the structural representation of process flow diagram of the present invention and device.
The specific embodiment:
Embodiment 1:
Directly utilize the ammonia source of 2% low concentration deposed ammonia of coking production, be used for sinter fume or fire coal boiler fume SO as absorbent 2Remove; In the inferior salt oxidizing process of two-stage oxidation, add Fe + 3, handle back flue gas qualified discharge, and the reclaim sulfuric acid ammonium.Detailed process is as follows:
1,130 ℃ of hot flue gas or boiler smoke (SO from steel sintering 2Concentration 1000mg-2000mg/Nm 3, dust-laden<200mg/Nm 3, electric precipitation or bag-type dust), enter the reverse jet tube of flue gas cooling and mother liquor concentration tower (7) from top with 20m/s gas speed, the reverse jet tube bottom upwards sprays into 50 ℃, density 1200g/m by nozzle 3The sulphur ammonium salt solution, liquid gas volume ratio L/G is 3/1000, after thermal insulation is cooled to 50 ℃ in the contrary spray of this turbulent flow tower, flue gas is discharged from flue gas cooling and mother liquor concentration tower (7) top and is entered top, absorption tower (2) reverse jet tube with 20m/s gas speed, form the foam absorption with total salt concentration 250g/L, basicity 5tt ° absorption mother liquor adverse current, volume ratio L/G=5/1000, absorptivity>95%, gas SO 2Qualified discharge;
2, bottom, absorption tower (2) is the absorption mother liquor circulating slot, and 2% coking ammonia water is directly mended in the Recycling Mother Solution groove of bottom, absorption tower (2), 5tt ° of absorption liquid basicity, pH value 5.5, density 1130g/cm 3, by absorption liquid circulating pump (3) circulation absorption mother liquor, absorption liquid delivery pump (5) is squeezed into nitrite oxidation column (8) with the absorption tower mother liquor of discharging. and blast air by air blast (6) to nitrite oxidation column (8) simultaneously and carry out oxidation, the amount that blasts air is by tower section 60m 3/ m 2.h calculate, inferior salt oxygenation efficiency>98%, residual gas imports flue gas cooling and mother liquor concentration tower (7) through the bubble-cap blast cap.Ammonium sulfate liquor circulating slot (9) is gone in the oxidation mother liquor overflow, by ammonium sulfate circulating pump (13) carry mother liquor by volume L/G=3/1000 deliver to flue gas cooling and mother liquor concentration tower (7) reverse jet tube bottom and the reverse spray of gas, the gas thermal insulation is cooled to 50 ℃, mother liquor is concentrated into 400g/L, the thickener mother liquor is delivered to filter (12) through sulphur ammonium liquid output filtering pump (11) and is filtered, again through evaporation, concentrate, behind the crystallizing and drying product.
3, catalyst Fe + 3Adding: the catalyst addition replenishes by the 0.01mol/L of absorption mother liquor discharge rate hourly, be made into 20% (mass concentration) aqueous solution, respectively absorption liquid circulating pump (3) and absorption liquid delivery pump (5) import department intermittently mend into, wherein: 1/3 of the aqueous solution mends absorption liquid circulating pump (3) inlet, and 2/3 of the aqueous solution mends absorption liquid delivery pump (5) inlet.
Embodiment 2:
Directly utilize the ammonia source of 10% low concentration deposed ammonia of coking production, be used for sinter fume or fire coal boiler fume SO as absorbent 2Remove; In the inferior salt oxidizing process of two-stage oxidation, add S 2O 3 -2, handle back flue gas qualified discharge, and the reclaim sulfuric acid ammonium.Detailed process is as follows:
1,140 ℃ of hot flue gas or boiler smoke (SO from steel sintering 2Concentration 2000mg-5000mg/Nm 3, dust-laden<200mg/Nm 3, electric precipitation or bag-type dust), enter the reverse jet tube of flue gas cooling and mother liquor concentration tower (7) from top with 22m/s gas speed, the reverse jet tube bottom upwards sprays into 50 ℃, density 1215g/m by nozzle 3The sulphur ammonium salt solution, liquid gas volume ratio L/G is 3/1000, after thermal insulation is cooled to 60 ℃ in the contrary spray of this turbulent flow tower, flue gas is discharged from flue gas cooling and mother liquor concentration tower (7) top and is entered top, absorption tower (2) reverse jet tube with 23m/s gas speed, form the foam absorption with total salt concentration 300g/L, basicity 10tt ° absorption mother liquor adverse current, volume ratio L/G=6/1000, absorptivity>95%, gas SO 2Qualified discharge.
2, bottom, absorption tower (2) is the absorption mother liquor circulating slot, and 10% coking ammonia water is directly mended in the Recycling Mother Solution groove of bottom, absorption tower (2), 10tt ° of absorption liquid basicity, pH value 5.8, density 1140g/cm 3, by absorption liquid circulating pump (3) circulation absorption mother liquor, absorption liquid delivery pump (5) is squeezed into nitrite oxidation column (8) with the absorption tower mother liquor of discharging, and blasts air by air blast (6) to nitrite oxidation column (8) simultaneously and carries out oxidation, and the amount that blasts air is by tower section 80m 3/ m 2.h calculate, inferior salt oxygenation efficiency>98%, residual gas imports flue gas cooling and mother liquor concentration tower (7) through the bubble-cap blast cap.Ammonium sulfate liquor circulating slot (9) is gone in the oxidation mother liquor overflow, by ammonium sulfate circulating pump (13) carry mother liquor by volume L/G=3/1000 deliver to flue gas cooling and mother liquor concentration tower (7) reverse jet tube bottom and the reverse spray of gas, the gas thermal insulation is cooled to 60 ℃, mother liquor is concentrated into 450g/L, the thickener mother liquor is delivered to filter (12) through sulphur ammonium liquid output filtering pump (11) and is filtered, again through evaporation, concentrate, behind the crystallizing and drying product.
3, catalyst S 2O 3 -2Adding: the catalyst addition replenishes by the 0.018mol/L of often hour absorption mother liquor discharge rate, be made into 20% (mass concentration) aqueous solution, respectively absorption liquid circulating pump (3) and absorption liquid delivery pump (5) import department intermittently mend into, wherein: 1/3 of the aqueous solution mends absorption liquid circulating pump (3) inlet, and 2/3 of the aqueous solution mends absorption liquid delivery pump (5) inlet.
Embodiment 3:
Directly utilize the ammonia source of 20% low concentration deposed ammonia of coking production, be used for sinter fume or fire coal boiler fume SO as absorbent 2Remove; In the inferior salt oxidizing process of two-stage oxidation, add Fe + 3, handle back flue gas qualified discharge, and the reclaim sulfuric acid ammonium.Detailed process is as follows:
1,150 ℃ of hot flue gas or boiler smoke (SO from steel sintering 2Concentration 3000mg-5000mg/Nm 3, dust-laden<200mg/Nm 3, electric precipitation or bag-type dust), enter the reverse jet tube of flue gas cooling and mother liquor concentration tower (7) from top with 27m/s gas speed, the reverse jet tube bottom upwards sprays into 50 ℃, density 1230g/m by nozzle 3The sulphur ammonium salt solution, liquid gas volume ratio L/G is 3/1000, after thermal insulation is cooled to 65 ℃ in the contrary spray of this turbulent flow tower, flue gas is discharged from flue gas cooling and mother liquor concentration tower (7) top and is entered top, absorption tower (2) reverse jet tube with 24m/s gas speed, form the foam absorption with total salt concentration 350g/L, basicity 15tt ° absorption mother liquor adverse current, volume ratio L/G=7/1000, absorptivity>95%, gas SO 2Qualified discharge.
2, bottom, absorption tower (2) is the absorption mother liquor circulating slot, and 20% coking ammonia water is directly mended in the Recycling Mother Solution groove of bottom, absorption tower (2), 15tt ° of absorption liquid basicity, pH value 6.2, density 1150g/cm 3By absorption liquid circulating pump (3) circulation absorption mother liquor, absorption liquid delivery pump (5) is squeezed into nitrite oxidation column (8) with the absorption tower mother liquor of discharging, and blasts air by air blast (6) to nitrite oxidation column (8) simultaneously and carries out oxidation, and the amount that blasts air is by tower section 100m 3/ m 2.h calculate, inferior salt oxygenation efficiency>98%, residual gas imports flue gas cooling and mother liquor concentration tower (7) through the bubble-cap blast cap.Ammonium sulfate liquor circulating slot (9) is gone in the oxidation mother liquor overflow, by ammonium sulfate circulating pump (13) carry mother liquor by volume L/G=3/1000 deliver to flue gas cooling and mother liquor concentration tower (7) reverse jet tube bottom and the reverse spray of gas, the gas thermal insulation is cooled to 65 ℃, mother liquor is concentrated into 500g/L, the thickener mother liquor is delivered to filter (12) through sulphur ammonium liquid output filtering pump (11) and is filtered, again through evaporation, concentrate, behind the crystallizing and drying product.
3, catalyst Fe + 3Adding: the catalyst addition replenishes by the 0.025mol/L of often hour absorption mother liquor discharge rate, be made into 20% (mass concentration) aqueous solution, respectively absorption liquid circulating pump (3) and absorption liquid delivery pump (5) import department intermittently mend into, wherein: 1/3 of the aqueous solution mends absorption liquid circulating pump (3) inlet, and 2/3 of the aqueous solution mends absorption liquid delivery pump (5) inlet.

Claims (2)

1, a kind of iron and steel, coal chemical enterprise waste coking ammonia water remove flue gas SO 2Technology, adopt ammonia process to absorb and inferior salt oxidation technology, the low concentration deposed ammonia of 2%-20% that it is characterized in that directly utilizing coking production is used for sinter fume or fire coal boiler fume SO as the ammonia source of absorbent 2Remove; In the inferior salt oxidizing process of two-stage oxidation, add Fe + 3Or S 2O 3 -2, handle back flue gas qualified discharge, the reclaim sulfuric acid ammonium; Detailed process is as follows:
A.130-150 ℃ hot flue gas or boiler smoke from iron and steel or coal chemical enterprise sintering enter with the reverse jet tube top of 20-27m/s gas speed from flue gas cooling and mother liquor concentration tower (7) top, and the reverse jet tube bottom upwards sprays into 50 ℃, density 1200-1230g/cm by nozzle 3The sulphur ammonium salt solution, liquid gas volume ratio L/G is 3/1000, after thermal insulation is cooled to 50-65 ℃ in the contrary spray of this turbulent flow tower, flue gas is from the flue gas cooling and discharge at mother liquor concentration tower (7) top and (2) top reverse jet tube enters from the absorption tower with 20-27m/s gas speed, form the foam absorption with the absorption mother liquor adverse current of total salt concentration 250-350g/L, basicity 5-15tt, volume ratio L/G=5/1000~7/1000, absorptivity>95%, gas SO 2Qualified discharge;
B. bottom, absorption tower (2) is the absorption mother liquor circulating slot, and the coking ammonia water of 2%-20% is directly mended in the Recycling Mother Solution groove of bottom, absorption tower (2), absorption liquid basicity 5-15tt, pH value 5.5-6.2, density 1130-1150g/cm 3By absorption liquid circulating pump (3) circulation absorption mother liquor, absorption liquid delivery pump (5) is squeezed into nitrite oxidation column (8) with the absorption tower mother liquor of discharging, and blasts air by air blast (6) to nitrite oxidation column (8) simultaneously and carries out chlorination, and the amount that blasts air is by tower section 60-100m 3/ m 2.h calculate, inferior salt oxygenation efficiency>98%, residual gas imports flue gas cooling and mother liquor concentration tower (7) through the bubble-cap blast cap; Ammonium sulfate liquor circulating slot (9) is gone in the oxidation mother liquor overflow, by ammonium sulfate circulating pump (13) by volume L/G=3/1000 carry mother liquor to flue gas cooling and mother liquor concentration tower (7) reverse jet tube lower end from shower nozzle to the reverse spray of gas, the gas thermal insulation is cooled to 50-65 ℃, mother liquor is concentrated into 400-500g/L, it is 6 o'clock that the thickener mother liquor adds ammoniacal liquor adjusting PH, deliver to filter (12) with sulphur ammonium liquid output filtering pump (11) and filter, again through evaporation, concentrate, behind the crystallizing and drying product;
C. catalyst Fe + 3Or S 2O 3 -2Adding: the catalyst addition replenishes by the 0.01-0.03mol/L of absorption mother liquor discharge rate hourly, be made into 20% aqueous solution, respectively absorption liquid circulating pump (3) and absorption liquid delivery pump (5) import department intermittently mend into, wherein: 1/3 of the aqueous solution mends absorption liquid circulating pump (3) inlet, and 2/3 of the aqueous solution mends absorption liquid delivery pump (5) inlet.
2, the device of the described process using of claim 1 is characterized in that this device is by ammoniacal liquor head tank (1), the absorption tower (2) that is connected with ammoniacal liquor head tank (1) by pipeline, place the absorption liquid circulating pump (3) and the absorption liquid delivery pump (5) of bottom, absorption tower (2) respectively, the catalyst solution groove (4) that is connected with the carrier pipe of absorption liquid circulating pump (3) and absorption liquid delivery pump (5) respectively, the nitrite oxidation column (8) that is connected with absorption liquid delivery pump (5) by pipeline and absorption tower (2), place the air blast (6) of nitrite oxidation column (8) bottom, by the cooling of pipeline and flue gas and mother liquor concentration tower (7) is connected and the bottom is provided with the ammonium sulfate liquor circulating slot (9) of star valve (10), the sulphur ammonium liquid output filtering pump (11) that is connected with star valve (10), the filter (12) that is connected with sulphur ammonium liquid output filtering pump (11), form with the ammonium sulfate circulating pump (13) that flue gas cooling and mother liquor concentration tower (7) are connected with ammonium sulfate liquor circulating slot (9) respectively by pipeline.
CNB2006100487018A 2006-09-29 2006-09-29 Process and apparatus for eliminating fume SO2 from waste coking ammonia water of iron and steel and coal chemical enterprise CN100430113C (en)

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CN101774610A (en) * 2010-03-04 2010-07-14 徐西征 Process method for producing ammonium sulfate in enterprises of coal-based synthetic natural gas
CN101991989A (en) * 2010-10-21 2011-03-30 武汉钢铁(集团)公司 Crystal bypass filtering method and device in single tower
CN102101006A (en) * 2011-01-21 2011-06-22 内蒙古庆华集团庆华煤化有限责任公司 Process for removing SO2 in smoke from boiler of coking plant by utilizing residual coked ammonia water
CN102228775A (en) * 2011-05-09 2011-11-02 云南亚太环境工程设计研究有限公司 Integrated method for desulphurization and defluorination of electrolytic aluminium flue gas
CN102258934A (en) * 2011-04-13 2011-11-30 云南亚太环境工程设计研究有限公司 Integrated desulfurization and dust removal method of petroleum coke calcining flue gas in carbon production for electrolytic aluminium
CN101804291B (en) * 2009-03-11 2012-05-30 杨立长 Impurity removal method of desulphurization by-product of sintering machine smoke subjected to ammonia method of steel enterprises
CN101632895B (en) * 2008-07-22 2012-06-27 解娟 Method for desulfurizing sintering flue gas
CN102527212A (en) * 2011-12-07 2012-07-04 南京钢铁股份有限公司 Comprehensive treating method and system for tail gas in ammoniac tank of coke-oven plant
CN102989294A (en) * 2012-11-26 2013-03-27 中国铝业股份有限公司 Aluminum electrolysis smoke treating method
CN104772022A (en) * 2015-02-05 2015-07-15 江西瑞林稀贵金属科技有限公司 Dynamic wave system used for treating combustion flue gas of electronic waste material
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Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1011303B (en) * 1988-02-08 1991-01-23 上海化工设计院 Method of purifying coke oven gas and getting ammonium hydrogen carbonate as by-product
US5624649A (en) * 1995-04-26 1997-04-29 General Electric Co. Process for reduction of sulfur dioxide emission from combustion gases combined with production of potassium sulfate
CN1086148C (en) * 1997-03-21 2002-06-12 沈阳环境科学研究所 New technology for absorbing and eliminating sulfur dioxide in smoke chemically
US6531104B1 (en) * 2000-11-21 2003-03-11 Alstom (Schweiz) Ag Process for the absorption of sulfur oxides and the production of ammonium sulfate

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CN101632895B (en) * 2008-07-22 2012-06-27 解娟 Method for desulfurizing sintering flue gas
CN101804291B (en) * 2009-03-11 2012-05-30 杨立长 Impurity removal method of desulphurization by-product of sintering machine smoke subjected to ammonia method of steel enterprises
CN101773778B (en) * 2010-01-04 2018-06-26 亚太环保股份有限公司 Method for integration of desulphurization and denitration of coal-fired flue gas by wet method
CN101774610A (en) * 2010-03-04 2010-07-14 徐西征 Process method for producing ammonium sulfate in enterprises of coal-based synthetic natural gas
CN101991989A (en) * 2010-10-21 2011-03-30 武汉钢铁(集团)公司 Crystal bypass filtering method and device in single tower
CN101991989B (en) * 2010-10-21 2013-04-24 武汉钢铁(集团)公司 Crystallization bypass filtering method and device in single tower
CN102101006B (en) * 2011-01-21 2013-08-28 内蒙古庆华集团庆华煤化有限责任公司 Process for removing SO2 in smoke from boiler of coking plant by utilizing residual coked ammonia water
CN102101006A (en) * 2011-01-21 2011-06-22 内蒙古庆华集团庆华煤化有限责任公司 Process for removing SO2 in smoke from boiler of coking plant by utilizing residual coked ammonia water
CN102258934A (en) * 2011-04-13 2011-11-30 云南亚太环境工程设计研究有限公司 Integrated desulfurization and dust removal method of petroleum coke calcining flue gas in carbon production for electrolytic aluminium
CN102258934B (en) * 2011-04-13 2013-12-04 云南亚太环境工程设计研究有限公司 Integrated desulfurization and dust removal method of petroleum coke calcining flue gas in carbon production for electrolytic aluminium
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CN102527212A (en) * 2011-12-07 2012-07-04 南京钢铁股份有限公司 Comprehensive treating method and system for tail gas in ammoniac tank of coke-oven plant
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CN102989294A (en) * 2012-11-26 2013-03-27 中国铝业股份有限公司 Aluminum electrolysis smoke treating method
CN104772022A (en) * 2015-02-05 2015-07-15 江西瑞林稀贵金属科技有限公司 Dynamic wave system used for treating combustion flue gas of electronic waste material

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