CN101543729A - Method suitable for utilization of resource of sintering flue gas desulphurization waste solution - Google Patents
Method suitable for utilization of resource of sintering flue gas desulphurization waste solution Download PDFInfo
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- CN101543729A CN101543729A CN200910029945A CN200910029945A CN101543729A CN 101543729 A CN101543729 A CN 101543729A CN 200910029945 A CN200910029945 A CN 200910029945A CN 200910029945 A CN200910029945 A CN 200910029945A CN 101543729 A CN101543729 A CN 101543729A
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- Prior art keywords
- ammonium sulfate
- ammonium sulphate
- feed liquid
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- concentration
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- 239000002699 waste material Substances 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 15
- 239000003546 flue gas Substances 0.000 title claims abstract description 15
- 238000005245 sintering Methods 0.000 title claims abstract description 12
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 75
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 69
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 68
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 239000002002 slurry Substances 0.000 claims abstract description 15
- 239000007787 solid Substances 0.000 claims abstract description 11
- 239000000243 solution Substances 0.000 claims abstract description 6
- 238000006477 desulfuration reaction Methods 0.000 claims description 20
- 230000023556 desulfurization Effects 0.000 claims description 20
- 238000001035 drying Methods 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 6
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 claims description 4
- 239000012266 salt solution Substances 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 3
- 230000008719 thickening Effects 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 abstract description 11
- 230000007613 environmental effect Effects 0.000 abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 3
- 239000001166 ammonium sulphate Substances 0.000 abstract 10
- 239000008187 granular material Substances 0.000 abstract 4
- 239000002562 thickening agent Substances 0.000 abstract 2
- 239000010413 mother solution Substances 0.000 abstract 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 6
- 239000010440 gypsum Substances 0.000 description 6
- 229910052602 gypsum Inorganic materials 0.000 description 6
- 230000003009 desulfurizing effect Effects 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 4
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 4
- 235000010261 calcium sulphite Nutrition 0.000 description 4
- 239000003337 fertilizer Substances 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000004087 circulation Effects 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical compound C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 206010013786 Dry skin Diseases 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- HQHVPDROXYYBFY-UHFFFAOYSA-N azane sulfane sulfuric acid Chemical compound S(=O)(=O)([O-])[O-].[SH3+].[NH4+] HQHVPDROXYYBFY-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000001473 noxious effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
- 239000012855 volatile organic compound Substances 0.000 description 1
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Abstract
The invention relates to a method suitable for utilization of resource of sintering flue gas desulphurization waste solution, belonging to the technology of utilizing resource of desulphurization waste solution for atmospheric pollution control in the environmental protection field. Desulphurization waste solution is delivered into a vortex separator (2) through an ammonium sulphate slurry pump (1) and a pipeline system so that solid and liquid are partially separated; low-concentration ammonium sulphate solution at the upper part of the vortex separator (2) is delivered into an ammonium sulphate feed liquid pot (9) through a pipeline, and high-concentration ammonium sulphate solution at the lower part of the vortex separator (2) is delivered into a thickener (3) through a pipeline; thickened high-solid ammonium sulphate solution enters a centrifuger (4) through an overflow pipeline arranged at the bottom of the thickener (3); ammonium sulphate granules with the water content of less than 5 percent is obtained, and ammonium sulphate mother solution enters the ammonium sulphate feed liquid pot (9); the ammonium sulphate granules enter a drier (5) and are dried by the drier (5), and ammonium sulphate granules with the water content of less than 1 percent are obtained; feed liquid in the ammonium sulphate feed liquid pot (9) is low-concentration ammonium sulphate slurry which returns to a desulphurization system through a feed liquid output pump (11) and reenters a dehydrating system so that high-concentration ammonium sulphate granules are prepared.
Description
Technical field
The present invention relates to field of environment protection air contaminant treatment desulfurization waste liquor application technology as the second resource, relate in particular to steel industry sintering flue gas ammonia method desulfurizing process for treating waste liquor.
Background technology
Existing similar technology process for treating waste liquor and good and bad the analysis:
1. limestone-gypsum wet desulphurization
Adopt lime stone slurry as desulfurizing agent, remove SO
2Generation contains the calcium sulfite waste liquid, and the calcium sulfite of generation changes into calcium sulfate in the compressed air oxygen in slurries pond, generates the end product gypsum, and this method is widely used in the means of flue gas desulfurization of power plant at present.
There is following defective in this method:
1) because China's gypsum resource is abundant, the gypsum market that desulfurization produces is poor, so be abandoned substantially, desulfurizing byproduct gypsum value is not high;
2) because desulfurated plaster can't utilize once more, the gypsum of bulk deposition is with land occupation and cause environmental pollution.
2 circulating fluidized bed dries
Flue gas advances the people from the bottom, absorption tower, reacts with the absorbent (calcium hydroxide), circulating ash (returning the absorption tower by the circulation skewed slot) and the water that add after Venturi tube is quickened, and removes the SO in the flue gas
x, HCl, HF, CO
2Deng gas.The generation main component is flying dust, calcium sulfite, calcium sulfate and the unreacted desulfurization ash of pulverized limestone completely.
There is following defective in this method:
1) the desulfurization ash main component of circulating fluidized bed dry is flying dust, calcium sulfite, a calcium sulfate and unreacted pulverized limestone completely, and the desulfurization ash economic worth is low, can't utilize;
2) through after fluid bed circulations up to a hundred time, noxious materials such as a large amount of heavy metal of enrichment, VOCs in the desulfurization ash are along with the increasingly stringent of environmental protection standard, even the lime-ash landfill also must be handled earlier.
Summary of the invention
Technical problem: the operation desulfurization product utilization rate that exists at above technology is low, secondary pollution problems is stacked, easily produced in a large amount of places of needs, the present invention proposes the method that a kind of suitable resource of sintering flue gas desulphurization waste solution utilizes, this method is utilized iron and steel enterprise's desulfurization waste liquor, mainly contain sulfurous acid (hydrogen) ammonium etc., by the fertile reparation technology of ammonium sulfate, production ammonium sulfate fertilizer, this accessory substance is for making the ammonium sulfate of agricultural fertilizer, not only realized " treatment of wastes with processes of wastes against one another ", and can also reach the purpose of " turning waste into wealth ".
Technical scheme: adopt desulfurization waste liquor as system ammonium sulfate raw material, the back utilizes the method for air aeration that ammonium bisulfite is oxidized to ammonium sulfate in reactor, after ammonium sulfate is discharged through producing ammonia sulfate crystal after filtration, dehydration, evaporation, the drying.Concrete grammar is as follows:
A). desulfurization waste liquor is by being delivered in the cyclone separator for ammonium sulfate slush pump and pipe-line system;
B). slurries reach the part Separation of Solid and Liquid in cyclone separator, top is contained the low-concentration sulfuric acid ammonium salt solution and is transported in the ammonium sulfate material liquid tank through pipeline, and the ammonium sulfate of bottom high concentration is transported in the stiff device through pipeline;
C). the solid ammonium sulfate of the height after the thickening of stiff device enters in the centrifuge through the overflow pipe of stiff device bottom;
D). the ammonium sulfate slurries continue Separation of Solid and Liquid in centrifuge, obtain moisture content and be lower than 5% ammonium sulfate, and ammonium sulfate liquor enters the ammonium sulfate material liquid tank;
E). ammonium sulfate enters drying machine, by the drying machine drying, obtains moisture content and is lower than 1% ammonium sulfate thing, and the hot-air that the thermal source of drying machine blasts by the air heater heater blower provides or directly logical steam provides;
F). the feed liquid in the ammonium sulfate material liquid tank is low-concentration sulfuric acid ammonium slurries, turns back to desulphurization system by the feed liquid rear pump, reenters dewatering system, with the ammonium sulfate of preparation high concentration.
Beneficial effect: owing to adopted above technical scheme, sintering flue gas ammonia method desulfurizing effluent resource of the present invention utilizes the accessory substance that technology is simple, system is reliable, utilize desulfurization waste liquor to make---ammonium sulfate quality height, can directly use as ammonium sulfate is fertile, the present invention has found the new technology of a suitable flue gas of sintering machine engineering circulation sustainable use, has reduced the overall operation expense of desulfurization project.Compare with other technologies, this technology utilization desulfurization waste liquor is prepared has higher quality, the better ammonium sulfate fertilizer of market, and the real low cost always pursued on the flue gas of sintering machine engineering of having accomplished has the target of output.This sintering device flue gas ammonia process of desulfurization effluent resource utilizes technology both to realize environmental benefit, has also realized economic benefit to a certain extent.
Description of drawings
Fig. 1 is the schematic diagram of sintering flue gas ammonia method desulfurizing waste liquid system ammonium sulfate of the present invention system.
Have among the figure: for ammonium sulfate slush pump 1, cyclone separator 2, stiff device 3, centrifuge 4, drying machine 5, packing machine 6, air heater 7, air blast 8, ammonium sulfate material liquid tank 9, material liquid tank agitator 10, feed liquid rear pump 11.
The specific embodiment
A) desulfurization waste liquor is by being delivered in the cyclone separator 2 for ammonium sulfate slush pump 1 and pipe-line system;
B) slurries reach the part Separation of Solid and Liquid in cyclone separator, and top is contained the low-concentration sulfuric acid ammonium salt solution and is transported in the ammonium sulfate material liquid tank 9 through pipeline, and the ammonium sulfate of bottom high concentration is transported in the stiff device 3 through pipeline;
C) the solid ammonium sulfate of the height after 3 thickenings of stiff device enters in the centrifuge 4 through the overflow pipe of stiff device bottom;
D) the ammonium sulfate slurries continue Separation of Solid and Liquid in centrifuge 4, obtain moisture content and are lower than 5% ammonium sulfate, and ammonium sulfate liquor enters ammonium sulfate material liquid tank 9;
E) ammonium sulfate enters drying machine 5, by drying machine 5 dryings, obtains moisture content and is lower than 1% ammonium sulfate thing, and the hot-air that the thermal source of drying machine 5 blasts by air heater 7 heater blowers 8 provides or directly logical steam provides;
F) use packing machine 6 the moisture content that obtains of drying be lower than 1% ammonium sulfate thing packing and preserve;
G) ammonium sulfate material liquid tank 9 is used to store the top low-concentration sulfuric acid ammonium salt solution of cyclone separator 2 and cyclone separator 2, stiff device 3, centrifuge 4 overflow slurry, a material liquid tank agitator 10 is installed in the ammonium sulfate serum pot 9, in this equipment, is solidified to prevent slurries;
H) feed liquid in the ammonium sulfate material liquid tank 9 is low-concentration sulfuric acid ammonium slurries, turns back to desulphurization system by feed liquid rear pump 11, reenters dewatering system, with the ammonium sulfate of preparation low-water-content.
Illustrate
Handling object is one of 198m2 sintering machine, exhaust gas volumn 800,000Nm3/h, 130 ℃ of flue-gas temperatures, SO2 concentration 1500mg/Nm3, ammonium sulfate 5.5t/h after the desulfurization (strength of fluid 15%).
Cyclone separator treating capacity 6m3/h goes into a concentration 150g/L, feed pressure 0.08～0.15MPa.Stiff device treating capacity, centrifuge processing amount 2.75t/h.Power of motor 5.5Kw.Dryer capacity 0.868t/h, ammonium sulfate output is 816.75t/h, ammonium sulfate content 99%.
The ammonium sulfate of producing has the following advantages:
1) desulfurization product ammonium sulfate quality is higher, can reach the agricultural ammonium sulfate primes of GB GB535-95 standard;
2) desulfurization product ammonium sulfate is the stronger chemical fertilizer of a kind of economy, and China's ammonium sulfate extensive market is taken off simultaneously Sulphur ammonium sulfate has preferably market.
Claims (1)
1. method that suitable resource of sintering flue gas desulphurization waste solution utilizes is characterized in that this method may further comprise the steps:
A). desulfurization waste liquor is by being delivered in the cyclone separator (2) for ammonium sulfate slush pump (1) and pipe-line system;
B). slurries reach the part Separation of Solid and Liquid in cyclone separator (2), top is contained the low-concentration sulfuric acid ammonium salt solution and is transported in the ammonium sulfate material liquid tank (9) through pipeline, and the ammonium sulfate of bottom high concentration is transported in the stiff device (3) through pipeline;
C). the solid ammonium sulfate of the height after stiff device (3) thickening enters in the centrifuge (4) through the overflow pipe of stiff device bottom;
D). the ammonium sulfate slurries continue Separation of Solid and Liquid in centrifuge (4), obtain moisture content and be lower than 5% ammonium sulfate, and ammonium sulfate liquor enters ammonium sulfate material liquid tank (9);
E). ammonium sulfate enters drying machine (5), by drying machine (5) drying, obtain moisture content and be lower than 1% ammonium sulfate thing, the hot-air that the thermal source of drying machine (5) blasts by air heater (7) heater blower (8) provides or directly logical steam provides;
F). the feed liquid in the ammonium sulfate material liquid tank (9) is low-concentration sulfuric acid ammonium slurries, turns back to desulphurization system by feed liquid rear pump (11), reenters dewatering system, with the ammonium sulfate of preparation high concentration.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100299455A CN101543729B (en) | 2009-03-25 | 2009-03-25 | Method suitable for utilization of resource of sintering flue gas desulphurization waste solution |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100299455A CN101543729B (en) | 2009-03-25 | 2009-03-25 | Method suitable for utilization of resource of sintering flue gas desulphurization waste solution |
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| Publication Number | Publication Date |
|---|---|
| CN101543729A true CN101543729A (en) | 2009-09-30 |
| CN101543729B CN101543729B (en) | 2012-03-21 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102976357A (en) * | 2012-12-28 | 2013-03-20 | 安徽工业大学 | Method for extracting ammonium sulfate from ammonia desulphurization wastewater by oxidation process |
| CN103011201A (en) * | 2012-12-28 | 2013-04-03 | 安徽工业大学 | Method for extracting ammonium thiocyanate from ammonia-process desulfurization waste liquid by oxidation process |
| CN103588340A (en) * | 2013-11-27 | 2014-02-19 | 安徽工业大学 | Method for treating sodium-alkali desulfurization waste liquid by causticization-acidification method |
| CN103896420A (en) * | 2014-04-13 | 2014-07-02 | 连芷萱 | Desulfurization waste water treatment system and method |
| CN104671258A (en) * | 2015-01-22 | 2015-06-03 | 张波 | Method for producing compound fertilizer by using byproduct ammonium sulfate generated during ammonia-process desulfurizing of flue gas of boiler |
| CN108514754A (en) * | 2018-03-29 | 2018-09-11 | 昆山三环保科技有限公司 | A kind of MVR novel crystallizations device goes out salt system |
| CN111249894A (en) * | 2018-11-30 | 2020-06-09 | 颜庭秀 | Method for simultaneously desulfurizing and denitrifying flue gas by using solid ammonium salt |
-
2009
- 2009-03-25 CN CN2009100299455A patent/CN101543729B/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102976357A (en) * | 2012-12-28 | 2013-03-20 | 安徽工业大学 | Method for extracting ammonium sulfate from ammonia desulphurization wastewater by oxidation process |
| CN103011201A (en) * | 2012-12-28 | 2013-04-03 | 安徽工业大学 | Method for extracting ammonium thiocyanate from ammonia-process desulfurization waste liquid by oxidation process |
| CN103011201B (en) * | 2012-12-28 | 2014-06-18 | 安徽工业大学 | Method for extracting ammonium thiocyanate from ammonia-process desulfurization waste liquid by oxidation process |
| CN102976357B (en) * | 2012-12-28 | 2014-08-13 | 安徽工业大学 | Method for extracting ammonium sulfate from ammonia desulphurization wastewater by oxidation process |
| CN103588340A (en) * | 2013-11-27 | 2014-02-19 | 安徽工业大学 | Method for treating sodium-alkali desulfurization waste liquid by causticization-acidification method |
| CN103588340B (en) * | 2013-11-27 | 2014-12-24 | 安徽工业大学 | Method for treating sodium-alkali desulfurization waste liquid by causticization-acidification method |
| CN103896420A (en) * | 2014-04-13 | 2014-07-02 | 连芷萱 | Desulfurization waste water treatment system and method |
| CN103896420B (en) * | 2014-04-13 | 2015-09-09 | 石家庄市西姆克科技有限责任公司 | Desulfurization wastewater treatment system and method |
| CN104671258A (en) * | 2015-01-22 | 2015-06-03 | 张波 | Method for producing compound fertilizer by using byproduct ammonium sulfate generated during ammonia-process desulfurizing of flue gas of boiler |
| CN108514754A (en) * | 2018-03-29 | 2018-09-11 | 昆山三环保科技有限公司 | A kind of MVR novel crystallizations device goes out salt system |
| CN111249894A (en) * | 2018-11-30 | 2020-06-09 | 颜庭秀 | Method for simultaneously desulfurizing and denitrifying flue gas by using solid ammonium salt |
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| Publication number | Publication date |
|---|---|
| CN101543729B (en) | 2012-03-21 |
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