CN201658945U - Sintering flue gas purification system based on heat pipe waste heat recovery technology - Google Patents
Sintering flue gas purification system based on heat pipe waste heat recovery technology Download PDFInfo
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- CN201658945U CN201658945U CN2010201764255U CN201020176425U CN201658945U CN 201658945 U CN201658945 U CN 201658945U CN 2010201764255 U CN2010201764255 U CN 2010201764255U CN 201020176425 U CN201020176425 U CN 201020176425U CN 201658945 U CN201658945 U CN 201658945U
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- 238000005245 sintering Methods 0.000 title claims abstract description 33
- 238000011084 recovery Methods 0.000 title claims abstract description 31
- 239000002918 waste heat Substances 0.000 title claims abstract description 27
- 238000005516 engineering process Methods 0.000 title claims description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title abstract description 12
- 239000003546 flue gas Substances 0.000 title abstract description 12
- 238000000746 purification Methods 0.000 title abstract description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 48
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 35
- 238000010521 absorption reaction Methods 0.000 claims abstract description 24
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 23
- 239000007788 liquid Substances 0.000 claims abstract description 22
- 230000003647 oxidation Effects 0.000 claims abstract description 20
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 20
- 239000007789 gas Substances 0.000 claims abstract description 19
- 238000003860 storage Methods 0.000 claims abstract description 6
- 238000001035 drying Methods 0.000 claims description 12
- 239000003034 coal gas Substances 0.000 claims description 7
- 238000004891 communication Methods 0.000 claims description 6
- 238000012546 transfer Methods 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 17
- 229910000831 Steel Inorganic materials 0.000 abstract description 7
- 239000010959 steel Substances 0.000 abstract description 7
- 229910052799 carbon Inorganic materials 0.000 abstract description 4
- 239000002699 waste material Substances 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 2
- 230000008859 change Effects 0.000 abstract description 2
- 230000000694 effects Effects 0.000 abstract description 2
- 238000002425 crystallisation Methods 0.000 abstract 2
- 230000008025 crystallization Effects 0.000 abstract 2
- 230000010485 coping Effects 0.000 abstract 1
- 239000000428 dust Substances 0.000 abstract 1
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 230000008719 thickening Effects 0.000 abstract 1
- 238000006477 desulfuration reaction Methods 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 13
- 230000023556 desulfurization Effects 0.000 description 13
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 12
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 12
- 235000011130 ammonium sulphate Nutrition 0.000 description 12
- 239000003517 fume Substances 0.000 description 10
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 235000011114 ammonium hydroxide Nutrition 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 5
- 239000000284 extract Substances 0.000 description 5
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 230000009615 deamination Effects 0.000 description 3
- 238000006481 deamination reaction Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000009413 insulation Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000012946 outsourcing Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical group C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 210000000481 breast Anatomy 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000010010 raising Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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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
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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Abstract
The utility model relates to a sintering flue gas purification system based on heat pipe waste heat recovery technique. The sintering machine is communicated with a heat pipe waste heat recovery device, and the recovery device is communicated with an electric dust collector, an induced draft fan, a regulating damper and a booster fan to a desulfurizing tower; the desulfurizing tower is communicated with the damper and the heat exchange device to the chimney; a gas interface is arranged in the absorption tower, and the absorption tower is communicated with the ammonia storage box and the ammonia adjusting box to the desulfurizing tower; the desulfurizing tower is communicated with the circulating liquid pool; the circulating liquid pool is communicated with a filter press which is communicated with a sintering machine; the circulating liquid pool is communicated with the oxidation pool, the filter, the multi-effect crystallization evaporator, the thickening tank, the centrifugal separator and the dryer; the oxidation fan is communicated with the circulating liquid pool; the heat pipe waste heat recovery device is respectively communicated with the heat exchange device, the absorption tower, the multi-effect crystallization evaporator and the dryer. Solves the pollution problem caused by steel production. The utility model discloses energy-conserving effect is showing, and the investment recovery period is short, to useless the control of waste, becomes useless for fertile, accords with present low carbon economy general requirement of coping with climate change.
Description
Technical field
The utility model relates to the energy-conserving and environment-protective technology that a kind of steel enterprise sintering machine flue gas is handled, particularly a kind of sintering gas purifying system based on the heat pipe heat recovery technology.
Background technology
Steel industry is as energy consumption rich and influential family, heavy polluter, and nearly material input over half is finally with the form output of waste gas, solid waste or byproduct.The SO that steel manufacture process produces
2Be mainly derived from sintering circuit, account for iron and steel enterprise's total emission volumn more than 70%, the energy consumption of sintering circuit is also very big simultaneously, accounts for 12% of metallurgical total energy consumption, and the waste heat of discharging accounts for 49% of wastage in bulk or weight heat energy.How to control SO in the sintering machine production process
2Discharging, be the SO of iron and steel enterprise
2Pollute the emphasis of control.
Before the utility model proposes, application number is that the patent of invention of 200910098231.X discloses a kind of " the sintering flue gas desulfurization combined coke-stove gas deamination circulation technology and the circulatory system ", and this patent is to utilize coke-stove gas deamination product-ammonium sulfite to deviate from SO in the sinter fume as desulfurizing agent
2, utilize desulfurization product-ammonium bisulfite to deviate from ammonia in the coke-stove gas then, thereby reach the desulfurization purpose of sinter fume as deamidization.But, in said system, fail effectively to utilize the waste heat of sinter fume discharging, a large amount of steam that will consume in follow-up sulfur removal technology and the preparation of sulphur ammonium need additionally obtain, and waste energy.In addition, adopt the low temperature ammonia-process desulfurization technique in the system, avoid the decomposition of ammonium bisulfite strictly to control desulfurization reaction temperature, thereby very easily produce the dew point corrosion problem, the stability and the reliability of system reduce greatly.
Application number is that the patent of invention of 200910103664.X discloses " a kind of sintering gas purifying and waste heat reclaiming process ", utilize the CFBB transformation of power plant for self-supply of existing steel mill, sinter fume pressurizeed send into after the preheating in the burner hearth and the lime stone reaction, thereby reach the purpose of sintering gas purifying.But adopt the method desulfurization, desulfuration efficiency will be starkly lower than the ammonia process of desulfurization, and the accessory substance utilization rate of desulfurization is not high, can produce a large amount of carbon dioxide in the burner hearth combustion process simultaneously, causes secondary pollution, does not meet current low-carbon economy requirement.
Summary of the invention
The purpose of this utility model just is to overcome above-mentioned defective, designs a kind of sintering gas purifying system based on the heat pipe heat recovery technology.
The technical solution of the utility model is:
Based on the sintering gas purifying system of heat pipe heat recovery technology, its major technique is characterised in that sintering machine is communicated with the heat pipe waste-heat recovery device, and the heat pipe waste-heat recovery device is communicated with electric cleaner, air-introduced machine, damper, booster fan to desulfurizing tower; Desulfurizing tower is communicated with damper, heat-exchanger rig to chimney; The coal gas interface is set in the absorption tower, and the absorption tower is communicated with storage ammonia case, transfers the ammonia case to desulfurizing tower; Desulfurizing tower communication loop liquid pool; The circulation liquid pool is communicated with filter press, and filter press is communicated with sintering machine; The circulation liquid pool is communicated with oxidation pond, filter, multiple-effect crystallizing evaporator, stiff jar, centrifugal separator to drying machine; Oxidation fan communication loop liquid pool; The heat pipe waste-heat recovery device is connected with heat-exchanger rig, absorption tower, multiple-effect crystallizing evaporator and drying machine respectively.
The sintering gas purifying system based on the heat pipe heat recovery technology that the utility model proposes mainly comprises four part process systems in its technical solution:
1. heat pipe residual neat recovering system: recycling sintering circuit secondary energy sources, adopt advanced person's heat pipe heat recovery technology efficiently, the low-grade exhaust sensible heat that is produced at sintering circuit back segment ring cooler, be that the tow taste heat of central cooler rear portion below 250 ℃ carries out used heat and utilize, do not influence the high-grade energy that the anterior delivery temperature of ring cooler can reach about 450 ℃ and recycle technology.The waste heat heat that is reclaimed can be used for producing steam to be used for desulfurization and the preparation of sulphur ammonium, and the while can add the smoke evacuation flue gas behind the thermal purification, avoids dew point corrosion.
2. desulfurizing agent generates (ammonia is washed in coking) system: the bottom of the coke-stove gas self-absorption tower that comes out from coke oven enters, and coal gas contacts with the phosphoric acid solution of circulated sprinkling at Ta Nei, and the NH3 in the coal gas is absorbed by solution.Coke-stove gas after the purification is discharged through top, absorption tower.Rich solution is pumped circulated sprinkling in tower with pump at the bottom of the tower behind the suction ammonia, and therefrom extracts a certain amount of rich solution to desorption system continuously out and regenerate.
3. sintering desulfuration system: the flue gas of drawing from the outlet of sintering machine air-introduced machine, after the booster fan supercharging, in desulfurizing tower, contact, fully after the reaction with the ammoniacal liquor of washing ammonia from coke-stove gas, flue gas after being purified drains into atmosphere through the exhaust pass at desulfurizing tower middle part by chimney.For guaranteeing under any operating mode, the flue-gas temperature of chimney breast 〉=80 ℃, the Steam Heating that system utilizes sintering waste heat to reclaim to produce purifies the back flue gas and is higher than dew-point temperature to guarantee exhaust gas temperature.
4. desulfurizing byproduct generation system: with contain the ammonium sulfurous solution that sulfur dioxide sinter fume reaction back generates and go out tower from the desulfurizing tower bottom, behind cyclone sediment, supernatant enters the oxidation of circulation liquid pool aeration, make heavy metal ion wherein form carbonate deposition, and oxidation part ammonium sulfite, circulation fluid circulates in circulating pump pumps into desulfurizing tower.After treating that ammonium sulfate concentrations in the pond reaches certain value, extract pump depth of drive oxidation pond by the sulphur ammonium, fully oxidation, the solution after separating enter the sulphur ammonium as ammonium sulfate liquor and extract workshop section.Ammonium sulfate liquor forms the ammonium sulfate finished product after handling through crystallizing evaporator, stiff jar, centrifugal separator and vibration fluidized bed drying.
The scheme that the utility model proposes is compared with other technologies has very significantly advantage:
1. make full use of the residual heat resources of sintering circuit, add waste-heat recovery device, energy-saving effect is remarkable, further reduces operating cost.Waste-heat recovery device adopts maturation hot pipe technique efficiently, its heat transfer efficiency height, and dependable performance, the investment payback time is short;
2. adopt the high temperature ammonia-process desulfurization technique, reaction temperature is not subjected to the influence of intermediate product, has reduced the generation of apparatus dew point corrosion to a great extent;
With the waste gas ammonia in the coke-stove gas and the sulfur dioxide in the sinter fume as the raw material of producing ammonium sulfate (desulfurizing byproduct), both save the expense of outsourcing desulfurizing agent, and changed the traditional sulfuric acid of coking again and washed ammonia process, saved the expense of outsourcing sulfuric acid, the treatment of wastes with processes of wastes against one another becomes useless in fertile;
4. this programme is the low carbon technique of standard, no CO
2Secondary pollutions such as discharging, the huge CO that is produced than the desulfurization of calcium method
2(desulfurization produces CO for 1 ton to exhaust emission
20.7 ton), more meet the low-carbon economy general requirement of present reply climate change.
Description of drawings:
Fig. 1---be system schematic of the present utility model.
Among Fig. 1, sintering machine 1, heat pipe waste-heat recovery device 2, electric cleaner 3, air-introduced machine 4, damper 5, booster fan 6, chimney 7, heat-exchanger rig 8, desulfurizing tower 9 is transferred ammonia case 10, storage ammonia case 11, absorption tower 12, coal gas interface 13, filter press 14, circulation liquid pool 15, oxidation fan 16, oxidation pond 17, filter 18, multiple-effect crystallizing evaporator 19, stiff jar 20, centrifugal separator 21, drying machine 22, ammonium sulfate finished product 23.
The specific embodiment:
The operation principle of the sintering flue gas ammonia method desulfurizing that the utility model adopted is:
With ammonia spirit as absorption liquid, the SO in the sinter fume
2With the ammoniacal liquor reaction, generate ammonium sulfite solution.Ammonium sulfite solution reaches the finite concentration rear oxidation, be condensed into ammonium sulfate is recovered.The main chemical reactions formula is as follows:
2NH
3·H
2O+SO
2→(NH
4)
2SO
3
(NH
4)
2SO
3+1/2O
2→(NH
4)
2SO
4
As shown in Figure 1:
In the utility model, sintering machine 1 is communicated with heat pipe waste-heat recovery device 2, and heat pipe waste-heat recovery device 2 is communicated with electric cleaner 3, air-introduced machine 4, damper 5, booster fan 6 to desulfurizing tower 9; Desulfurizing tower 9 is communicated with damper 5, heat-exchanger rig 8 to chimney 7; Coal gas interface 13 is set in the absorption tower 12, and absorption tower 12 is communicated with storage ammonia case 11, transfers ammonia case 10 to desulfurizing tower 9; Desulfurizing tower 9 communication loop liquid pools 15; Circulation liquid pool 15 is communicated with filter press 14, and filter press 14 is communicated with sintering machine 1; The circulation liquid pool is communicated with oxidation pond 17, filter 18, multiple-effect crystallizing evaporator 19, stiff jar 20, centrifugal separator 21 to drying machine 22, goes out ammonium sulfate finished product 23; Oxidation fan 16 communication loop liquid pools 14; Heat pipe waste-heat recovery device 2 is connected with heat-exchanger rig 8, absorption tower 12, multiple-effect crystallizing evaporator 19 and drying machine 22 respectively.
The utility model illustrates in working order:
After sinter fume at first comes out from sintering machine 1, deliver to heat pipe waste-heat recovery device 2 through the insulation flue and carry out waste heat recovery, and make the steam generator of heat pipe waste-heat recovery device 2 produce heat-exchanger rig 8, absorption tower 12, multiple-effect crystallizing evaporator 19 and drying machine 22 needed steam; Sinter fume after the cooling is delivered to electric cleaner 3 through the insulation flue and is carried out dedusting, through air-introduced machine 4 is delivered to booster fan 6 pressurizations by damper 5 after, enters and carries out desulphurization reaction in the desulfurizing tower 9 then; Flue gas is delivered to damper 6 through the exhaust pass at desulfurizing tower 9 middle parts after desulfurizing tower 9 internal reaction desulfurization, drain into atmosphere by chimney 7 behind heat-exchanger rig 8 heat temperature raisings.
Enter from the coal gas interface 13 of coke-stove gas self-absorption tower 12 bottoms that coke oven comes out, in absorption tower 12, contact, wash ammonia through phosphoric acid and produce desulfurizing agent ammoniacal liquor with the phosphoric acid solution of circulated sprinkling; For the ammoniacal liquor quality of guaranteeing that deamination forms, must filter removal impurity to the resident liquid in 12 bottoms, absorption tower, rich solution is pumped to absorption tower 12 with pump and is recycled at the bottom of 12 towers of absorption tower; The absorption tower required steam of 12 reactions is provided by heat pipe waste-heat recovery device 2; Coke-stove gas is washed the desulfurizing agent ammoniacal liquor that ammonia produces and is stored in the storage ammonia case 11, with after after transferring ammonia case 10 to adjust pH and concentration, send into and carry out desulphurization reaction in the desulfurizing tower 9.
Go out tower with the ammonium sulfurous solution that contains sulfur dioxide sinter fume reaction back generation from desulfurizing tower 9 bottoms, behind cyclone sediment, supernatant enters the 15 aeration oxidations of circulation liquid pool, provide the sufficient amount of oxygen reaction by oxidation fan 16, make heavy metal ion wherein form carbonate deposition, and oxidation part ammonium sulfite; Precipitation is delivered to filter press 14 by turbid liquid pump and is compressed to clod, returns in the sintering machine 1 and utilizes; Circulation fluid circulates in circulating pump pumps into desulfurizing tower 9, treat that ammonium sulfate concentrations in the pond reaches certain value after, extract pump by the sulphur ammonium and squeeze into oxidation pond 17, fully oxidation, the solution after separating enter the sulphur ammonium as ammonium sulfate liquor and extract workshop section; Ammonium sulfate liquor forms ammonium sulfate finished product 23 outputs after handling through filter 18, multiple-effect crystallizing evaporator 19, stiff jar 20, centrifugal separator 21 and drying machine 22.Multiple-effect crystallizing evaporator 19 and drying machine 22 required steam in service are provided by heat pipe waste-heat recovery device 2.
The vapor portion that is produced by heat pipe waste-heat recovery device 2 is used to provide absorption tower 12 interior satisfied operations required; part is used to provide multiple-effect crystallizing evaporator 19 and drying machine 22 to move required; part is used to feed that heat-exchanger rig 8 heats flue gas after being purified so that its temperature is higher than dew-point temperature, and the generation of effectively avoiding dew point corrosion is with protection chimney 7.
Claims (1)
1. based on the sintering gas purifying system of heat pipe heat recovery technology, it is characterized in that sintering machine is communicated with the heat pipe waste-heat recovery device, the heat pipe waste-heat recovery device is communicated with electric cleaner, air-introduced machine, damper, booster fan to desulfurizing tower; Desulfurizing tower is communicated with damper, heat-exchanger rig to chimney; The coal gas interface is set in the absorption tower, and the absorption tower is communicated with storage ammonia case, transfers the ammonia case to desulfurizing tower; Desulfurizing tower communication loop liquid pool; The circulation liquid pool is communicated with filter press, and filter press is communicated with sintering machine; The circulation liquid pool is communicated with oxidation pond, filter, multiple-effect crystallizing evaporator, stiff jar, centrifugal separator to drying machine; Oxidation fan communication loop liquid pool; The heat pipe waste-heat recovery device is connected with heat-exchanger rig, absorption tower, multiple-effect crystallizing evaporator and drying machine respectively.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102614735A (en) * | 2012-04-13 | 2012-08-01 | 大连华氏流体设备有限公司 | Device and method for smoke desulphurization and waste recycle |
| CN102936651A (en) * | 2012-10-23 | 2013-02-20 | 鞍钢股份有限公司 | Sintering simultaneous desulfurization and denitrification system and desulfurization and denitrification method thereof |
| CN103170208A (en) * | 2013-03-25 | 2013-06-26 | 哈尔滨工程大学 | Emission device for reducing emission of smoke pollutants |
| CN104624011A (en) * | 2015-02-11 | 2015-05-20 | 湖州宜可欧环保科技有限公司 | Flue gas treatment system |
| CN105126581A (en) * | 2015-08-07 | 2015-12-09 | 无锡桥阳机械制造有限公司 | Method for desulfurization with coking gas washing deamination ammonia water |
| CN105688565A (en) * | 2016-02-04 | 2016-06-22 | 云南旭光节能有限公司 | Metallurgical mine calcining tail gas purifying and heat recycling device and process |
| CN106362569A (en) * | 2016-08-26 | 2017-02-01 | 江苏中圣高科技产业有限公司 | Ammonia-process desulfurization device and method for stepwise recycling of residual heat of high-temperature flue gas |
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2010
- 2010-04-30 CN CN2010201764255U patent/CN201658945U/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102614735A (en) * | 2012-04-13 | 2012-08-01 | 大连华氏流体设备有限公司 | Device and method for smoke desulphurization and waste recycle |
| CN102936651A (en) * | 2012-10-23 | 2013-02-20 | 鞍钢股份有限公司 | Sintering simultaneous desulfurization and denitrification system and desulfurization and denitrification method thereof |
| CN102936651B (en) * | 2012-10-23 | 2015-10-07 | 鞍钢股份有限公司 | Sintering simultaneous desulfurization and denitrification system and desulfurization and denitrification method thereof |
| CN103170208A (en) * | 2013-03-25 | 2013-06-26 | 哈尔滨工程大学 | Emission device for reducing emission of smoke pollutants |
| CN103170208B (en) * | 2013-03-25 | 2015-03-11 | 哈尔滨工程大学 | Emission device for reducing emission of smoke pollutants |
| CN104624011A (en) * | 2015-02-11 | 2015-05-20 | 湖州宜可欧环保科技有限公司 | Flue gas treatment system |
| CN104624011B (en) * | 2015-02-11 | 2017-07-28 | 浙江宜可欧环保科技有限公司 | A kind of smoke processing system |
| CN105126581A (en) * | 2015-08-07 | 2015-12-09 | 无锡桥阳机械制造有限公司 | Method for desulfurization with coking gas washing deamination ammonia water |
| CN105688565A (en) * | 2016-02-04 | 2016-06-22 | 云南旭光节能有限公司 | Metallurgical mine calcining tail gas purifying and heat recycling device and process |
| CN106362569A (en) * | 2016-08-26 | 2017-02-01 | 江苏中圣高科技产业有限公司 | Ammonia-process desulfurization device and method for stepwise recycling of residual heat of high-temperature flue gas |
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