CN101254392A - Energy-saving type sodium sulphite circulation desulfurizing device and method - Google Patents
Energy-saving type sodium sulphite circulation desulfurizing device and method Download PDFInfo
- Publication number
- CN101254392A CN101254392A CNA2007100782507A CN200710078250A CN101254392A CN 101254392 A CN101254392 A CN 101254392A CN A2007100782507 A CNA2007100782507 A CN A2007100782507A CN 200710078250 A CN200710078250 A CN 200710078250A CN 101254392 A CN101254392 A CN 101254392A
- Authority
- CN
- China
- Prior art keywords
- communicates
- absorption liquid
- breakdown
- circulating slot
- liquid circulating
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 title claims abstract description 91
- 235000010265 sodium sulphite Nutrition 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 25
- 230000003009 desulfurizing effect Effects 0.000 title claims description 63
- 238000010521 absorption reaction Methods 0.000 claims abstract description 127
- 239000007788 liquid Substances 0.000 claims abstract description 105
- 239000000779 smoke Substances 0.000 claims abstract description 38
- 238000005406 washing Methods 0.000 claims abstract description 33
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims abstract description 29
- 230000023556 desulfurization Effects 0.000 claims abstract description 28
- 238000006243 chemical reaction Methods 0.000 claims abstract description 22
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 18
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 claims abstract description 7
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 claims abstract description 7
- 230000015556 catabolic process Effects 0.000 claims description 58
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 56
- 239000003546 flue gas Substances 0.000 claims description 56
- 239000011734 sodium Substances 0.000 claims description 55
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical group [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 45
- 239000007789 gas Substances 0.000 claims description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 35
- 239000003795 chemical substances by application Substances 0.000 claims description 21
- 239000007921 spray Substances 0.000 claims description 15
- 239000000706 filtrate Substances 0.000 claims description 12
- 230000002745 absorbent Effects 0.000 claims description 11
- 239000002250 absorbent Substances 0.000 claims description 11
- 238000013019 agitation Methods 0.000 claims description 10
- 230000008676 import Effects 0.000 claims description 10
- 238000002360 preparation method Methods 0.000 claims description 10
- 239000008234 soft water Substances 0.000 claims description 10
- 238000003756 stirring Methods 0.000 claims description 10
- CBCKQZAAMUWICA-UHFFFAOYSA-N 1,4-phenylenediamine Chemical compound NC1=CC=C(N)C=C1 CBCKQZAAMUWICA-UHFFFAOYSA-N 0.000 claims description 8
- 239000003963 antioxidant agent Substances 0.000 claims description 8
- 230000003078 antioxidant effect Effects 0.000 claims description 8
- 230000008901 benefit Effects 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 239000011593 sulfur Substances 0.000 claims description 6
- 229910052717 sulfur Inorganic materials 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 4
- 239000003317 industrial substance Substances 0.000 claims description 4
- 150000005208 1,4-dihydroxybenzenes Chemical class 0.000 claims description 3
- 239000006227 byproduct Substances 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000007710 freezing Methods 0.000 claims description 3
- 230000008014 freezing Effects 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 229940079827 sodium hydrogen sulfite Drugs 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 abstract description 2
- 239000006096 absorbing agent Substances 0.000 abstract 2
- 239000000243 solution Substances 0.000 description 21
- 239000008367 deionised water Substances 0.000 description 7
- 229910021641 deionized water Inorganic materials 0.000 description 7
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 229910000019 calcium carbonate Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 2
- 108010085603 SFLLRNPND Proteins 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241001274216 Naso Species 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000006213 oxygenation reaction Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000007115 recruitment Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention relates to an energy-saving sodium sulfite circulation and desulfurization device as well as the method thereof, the desulfurization device comprises a desulfurization tower as well as a first and a second absorption liquid circulation grooves, the top part of the desulfurization tower communicates with a chimney, the lower part of the desulfurization tower communicates with the top part of a washing and cooling tower, and the bottom part of the washing and cooling tower is communicated with a circulation washing groove. The invention is characterized in that the washing and cooling tower communicates with a heat exchanger, which then communicates with a flue after communicating with a decomposed jacket reactor; the second absorption liquid circulation groove is communicated with a coil pipe in the heat exchanger, and the coil pipe is communicated with the reaction chamber of the decomposed jacket reactor; the lower part of the decomposed jacket reactor is communicated with a centrifuge. The invention has the desulfurization steps as follows: initial absorption liquid is prepared, the temperature of smoke is reduced, sulfur dioxide is absorbed, sodium bisulfite is decomposed, and sodium sulfite is recycled. The waste heat of the smoke is fully utilized, initial absorber is changed into circulation absorber to be used, the running cost is reduced, and the environment protection is favored.
Description
Technical field
The present invention relates to fume desulphurization method, be specifically related to energy-saving type sodium sulphite circulation desulfurizing device and method.
Background technology
Account for more than 70% of the disposable energy at China's fire coal, owing to contain sulphur in the coal, so the burning back produces a large amount of SO
2Thereby, cause serious atmosphere pollution.Therefore, the task of flue gas desulfurization is very heavy.At present, flue gas being carried out the desulfurization processing is to reduce SO
2The effective method of discharging and acid rain formation, the wet process of FGD technology of successful operation has comparative advantage with the calcium method.The calcium method is an absorbent with calcium carbonate (being lime stone), and its chemical reaction is as follows:
CaCO
3+SO
2+1/2H
2O＝CaSO
3·1/2H
2O+CO
2↑
2CaSO
3·1/2H
2O+3H
2O＝2CaSO
4·2H
2O
Calcium carbonate (being lime stone) is water-soluble very low material, during as absorbent, is that it is ground into 300 purpose powder, forms with water that slurries implement.Since solid matter is arranged, very high to the requirement of spraying apparatus and conveying equipment.Absorb SO
2After product C aSO
3And the CaSO that generates after the oxidation
4, all be the very little material of solubility, easy blocking pipe and equipment.Therefore, the calcium carbonate price is low though the calcium method has, technology maturation, advantage that desulfuration efficiency is high, has technology and equipment more complicated, fund input is big, operating cost is high shortcoming.Still be in lossing state aspect economic benefit, power plant has to take to raise the measure of electricity price lattice in order to reduce loss.So, seek a kind ofly can alleviate the fume desulphurization method that environmental pollution can significantly reduce operating cost again, be long-standing objective demand.CN1660474A discloses the application for a patent for invention that name is called " wet fuel gas desulfurizing technology ", and it can handle sulfurous fuels burning back acidic gas in flue gas (SO
2).Its principle is by alkaline desulfurizing agent-sodium sulfite solution and sulfur in smoke reaction, reaches the purpose that purifies flue gas, and sodium sulfite solution is renewable recycling.This wet fuel gas desulfurizing technology has the absorption system non-scaling, and pipeline, equipment do not stop up, the desulfuration efficiency height, and liquid-gas ratio is low, the advantage that whole system operating cost is low.But when the regeneration sodium sulfite, used certain density milk of lime, neutralization reaction generates NaSO
3With sediment CaSO
3And CaSO
4, needing will can be recycling to the sodium sulfite of regeneration through separating treatment, but also will handle the sediment of generation.In addition, also insufficient to the afterheat utilization of flue gas.
Summary of the invention
The purpose of this invention is to provide a kind of energy-saving type sodium sulphite circulation desulfurizing device and method, the corollary equipment of its device is not easy to stop up, and can guarantee that flow process is unimpeded, and Maintenance and Repair are convenient; Its method is to utilize fume afterheat as the needed energy of absorbent regeneration, the desulfuration efficiency height, and reacted product can both be used easily, and is little to the pollution of environment, and can significantly reduce operating cost.
Energy-saving type sodium sulphite circulation desulfurizing device of the present invention comprises desulfurizing tower, is located at the desulfurizing tower outer first absorption liquid circulating slot and the second absorption liquid circulating slot, and the inside of desulfurizing tower is divided into three districts, upper, middle and lower at interval by twice; The district is provided with first shower nozzle that communicates with the first absorption liquid circulating slot on desulfurizing tower inside, and bottom in district communicates with the first absorption liquid circulating slot on this; Be provided with second shower nozzle that communicates with the second absorption liquid circulating slot in the middle district of desulfurizing tower inside, the bottom of distinguishing in this communicates with the second absorption liquid circulating slot; The bottom of the first absorption liquid circulating slot communicates with the second absorption liquid circulating slot; The exhanst gas outlet at desulfurizing tower top communicates with chimney, the smoke inlet of desulfurizing tower bottom communicates with the exhanst gas outlet of washing cooling top of tower, the bottom of washing cooling tower communicates with the recirculated water washing trough, and the 3rd shower nozzle that communicates with the recirculated water washing trough is located at the top in the washing cooling tower; It is characterized in that:
The smoke inlet of a, washing cooling tower bottom communicates with the exhanst gas outlet of a heat exchanger bottom at least, the smoke inlet on heat exchanger top communicates with the exhanst gas outlet of breakdown jacket reactor side, and the smoke inlet of breakdown jacket reactor side communicates with flue;
Coiled pipe in the outlet of b, the second absorption liquid circulating slot bottom and the heat exchanger communicates, and the outlet of coiled pipe communicates with the reative cell of breakdown jacket reactor; The outlet of the reactor top of breakdown jacket reactor communicates with the import of condenser, and the outlet of condenser communicates with the import of moisture trap;
The bottom of c, breakdown jacket reactor communicates with a desk centrifuge, and the outlet of centrifuge communicates with the reative cell of breakdown jacket reactor.
The breakdown jacket reactor of described energy-saving type sodium sulphite circulation desulfurizing device comprises: the tubulation that reative cell, an end are connected with reative cell, the discharge bucket that is connected with the other end of tubulation, be connected the chuck of reative cell and tubulation side; Smoke inlet on the chuck communicates with flue, and the lower end of discharge bucket communicates with centrifuge.The structure and the ZL200520009573.7 utility model patent of " breakdown jacket reactor " that the present invention uses are basic identical, just in kettle, set up tubulation, to strengthen the heat exchange effect, still kept installation and removal convenient, the characteristics of easy maintenance, when the dust in the flue gas is deposited in the chuck morely, can dismantles chuck easily and remove dust, to guarantee the heat exchange effect.
Described energy-saving type sodium sulphite circulation desulfurizing device, the smoke inlet of its washing cooling tower bottom communicates with the exhanst gas outlet of two heat exchanger bottoms, the smoke inlet on two heat exchanger tops communicates with the exhanst gas outlet of two breakdown jacket reactor sides respectively, and the smoke inlet of two breakdown jacket reactor bottoms communicates with flue respectively;
The outlet of the second absorption liquid circulating slot bottom communicates with coiled pipe in two heat exchangers respectively, and the outlet of two coiled pipes communicates with the reative cell of two breakdown jacket reactors respectively; The outlet of the reactor top of two breakdown jacket reactors communicates with the import of condenser respectively, and the outlet of condenser communicates with the import of moisture trap;
The discharge bucket of the bottom of two breakdown jacket reactors communicates with a desk centrifuge respectively, and the outlet of two desk centrifuges communicates with the reative cell of two breakdown jacket reactors respectively.
This programme is provided with two heat exchangers and two breakdown jacket reactors, and it acts on except the temperature of rapid reduction flue gas, can also be when breakdown jacket reactor of maintenance, and another works on, and carries out continuously to keep desulfurization.
Energy-saving type sodium sulphite circulation desulfurization method of the present invention is carried out on energy-saving type sodium sulphite circulation desulfurizing device, and its step is as follows:
The first step, preparation initial absorption liquid: the initial absorption agent is Na
2CO
3, soft water (deionized water) is added in the first absorption liquid circulating slot, under agitation add Na gradually
2CO
3, the weight percent concentration that makes it in solution is 8-18%, fully after the dissolving, adds solution weight 0.05% antioxidant again, stirs all;
Second step, circulation initial absorption liquid: the circulating pump of opening the first absorption liquid circulating slot and the second absorption liquid circulating slot, make absorption liquid spray into going up of desulfurizing tower inside and distinguish, get back to the first absorption liquid circulating slot, Na from the bottom in this district again by first shower nozzle that communicates with the first absorption liquid circulating slot
2CO
3Solution flows into the second absorption liquid circulating slot from the bottom of the first absorption liquid circulating slot; Make absorption liquid spray into the middle district of desulfurizing tower inside by second shower nozzle that communicates with the second absorption liquid circulating slot simultaneously, the second absorption liquid circulating slot is got back in the bottom of distinguishing from this again;
The 3rd step, flue gas cool-down: the temperature that flue is discharged be approximately 180 ℃ flue gas from the smoke inlet of " breakdown jacket reactor " side enter the chuck and tubulation between carry out heat exchange; Flue gas after temperature descends enters heat exchanger from the exhanst gas outlet of " breakdown jacket reactor " and carries out heat exchange once more, and the flue gas that reduces once more after the temperature is discharged from the exhanst gas outlet of heat exchanger, and enters in it from the smoke inlet of washing cooling tower bottom; Water in the wash water circulating slot sprays from the top of washing in the cooling tower from shower nozzle through water pump, further reduces the temperature of flue gas, to below 60 ℃;
The 4th step, absorb sulfur dioxide: the flue gas that temperature is reduced to below 60 ℃ is discharged from the exhanst gas outlet of washing cooling top of tower, enter inferior segment in it from the smoke inlet of desulfurizing tower bottom again, flue gas carries out reasonable distribution in this district, equably from first the shade of each riser at interval enter desulfurizing tower the district, contact the part SO in the flue gas with the absorption liquid of second shower nozzle spray that is located at Zhong Qu top
2Be absorbed; Flue gas enters the district of desulfurizing tower from second the shade of each riser at interval, and is located at the absorption liquid that first shower nozzle of distinguishing top sprays and contacts the remaining SO in the flue gas
2The overwhelming majority is absorbed, and then, enters the chimney discharging from the exhanst gas outlet at desulfurizing tower top; Following chemical reaction takes place:
Na
2CO
3+SO
2＝Na
2SO
3+CO
2↑
Sodium sulfite that obtains with reaction and the SO in the flue gas
2It is as follows to react:
Na
2SO
3+SO
2+H
2O＝2NaHSO
3
The 5th step, decompose sodium hydrogensulfite: the solution of sodium bisulfite that absorption liquid and sulfur in smoke reaction generate, pump into coiled pipe in the heat exchanger through water pump from the second absorption liquid circulating slot, after preheating, enter in the reative cell of breakdown jacket reactor, in the chuck of breakdown jacket reactor, reach the flue gas heating between tubulation again, take place to decompose as follows:
2NaHSO
3→Na
2SO
3+SO
2↑+H
2O
In the 6th step, separate the sulfur dioxide in the steam: the 5th step was decomposed the SO that generates
2Discharge from the reative cell outlet at breakdown jacket reactor top, enter the condenser cooling again, make SO
2Most of water vapor condensation in the gas is a water, then, discharges from the outlet of condenser, enters moisture trap, carry out gas-water separation after, with SO
2Gas is sent to liquefaction and is handled, as industrial chemicals;
In the 7th step, recycling sodium sulfite: the 5th step was decomposed the Na that generates
2SO
3And H
2O is discharged into centrifuge from the discharge bucket of breakdown jacket reactor bottom to be separated; The centrifuge separation is obtained Na
2SO
3Solid to add the first absorption liquid circulating slot recycling in addition as the circulation absorbent;
In the 8th step, separating filtrate is handled: contain NaHSO in the 7th filtrate that goes on foot under taking advantage of
3, Na
2SO
3And Na
2SO
4, pump into again in the reative cell of breakdown jacket reactor, make NaHSO wherein
3Decompose; Na in separating filtrate
2SO
4Content reach at 5% o'clock, separating filtrate is sent to freezing and crystallizing, isolate byproduct Na
2SO
4
Described energy-saving type sodium sulphite circulation desulfurization method, the initial absorption agent is NaOH, the first step, preparation initial absorption liquid: soft water is added in the first absorption liquid circulating slot, under agitation add NaOH gradually, the weight percent concentration that makes it in solution is 7-14%, fully after the dissolving, add solution weight 0.05% antioxidant again, stir all; Following chemical reaction takes place:
2NaOH+SO
2→Na
2SO
3+H
2O
Sodium sulfite that obtains with reaction and the SO in the flue gas
2It is as follows to react:
Na
2SO
3+SO
2+H
2O＝2NaHSO
3
All the other steps are identical with last method.
Described energy-saving type sodium sulphite circulation desulfurization method, the antioxidant that adds in the absorption liquid is p-phenylenediamine (PPD) or hydroquinones.Since oxidation, the Na of fraction
2SO
3Be oxidized into Na
2SO
4, the effect that adds antioxidant is that the oxygenation efficiency that makes is reduced to below 5%, thereby reduces the magnitude of recruitment of initial absorption agent, reduces cost.
Described energy-saving type sodium sulphite circulation desulfurization method, when the circulation absorbent after loss appears in desulfurization, need in time to replenish initial absorption agent Na
2CO
3, or NaOH, to keep the desulphurizing ability of absorption liquid.
The present invention compares with prior art and has the following advantages: the waste heat of flue gas is fully used, making the reacted product of initial absorption agent and sulfur dioxide change the circulation absorbent into is used, the accessory substance that obtains after the desulfurization is convenient to utilize, can be used as commodity selling, thereby significantly reduced the operating cost of desulfurization; Initial absorption agent, circulation absorbent and accessory substance all are water-soluble good materials, can not cause equipment to stop up in technical process, can guarantee that flow process is unimpeded; The desulfuration efficiency height generally can reach more than 95%, helps environmental protection.
Description of drawings
Fig. 1 is the energy-saving type sodium sulphite circulation desulfurizing device schematic diagram.
The specific embodiment
The invention will be further described below in conjunction with accompanying drawing.
Embodiment one: sodium carbonate is adopted in the initial absorption agent, by energy-saving type sodium sulphite circulation desulfurizing device flue gas is carried out desulfurization and handles.
Referring to Fig. 1, the inside of the desulfurizing tower 1 of energy-saving type sodium sulphite circulation desulfurizing device is divided into three districts, upper, middle and lower at interval with twice, the first absorption liquid circulating slot 2 and the second absorption liquid circulating slot 3 are located at the outside of desulfurizing tower, the bottom of distinguishing on the desulfurizing tower communicates with the first absorption liquid circulating slot, the bottom of distinguishing in the desulfurizing tower communicates with the second absorption liquid circulating slot, and the bottom of the first absorption liquid circulating slot communicates with the second absorption liquid circulating slot; The first shower nozzle 2-1 that communicates with the first absorption liquid circulating slot is installed in the top of distinguishing on the desulfurizing tower inside, and the second shower nozzle 3-1 that communicates with the second absorption liquid circulating slot is installed in the top of distinguishing in the desulfurizing tower inside; The smoke inlet of desulfurizing tower bottom communicates with the exhanst gas outlet at washing cooling tower 4 tops, and the exhanst gas outlet at desulfurizing tower top communicates with chimney, and the flue gas after the desulfurization is discharged from chimney;
The bottom of washing cooling tower 4 communicates with recirculated water washing trough 5, and the 3rd shower nozzle 5-1 that communicates with the recirculated water washing trough is installed in the top in the washing cooling tower; The smoke inlet of washing cooling tower bottom communicates with the exhanst gas outlet of two heat exchanger 6 bottoms, the smoke inlet on two heat exchanger tops communicates with the exhanst gas outlet on top, two breakdown jacket reactor 7 sides respectively, and the smoke inlet of bottom, two breakdown jacket reactor sides communicates with flue respectively;
The outlet of the second absorption liquid circulating slot, 3 bottoms communicates with coiled pipe in two heat exchangers 6 respectively, and the outlet of two coiled pipes communicates with the reative cell 7-1 of two breakdown jacket reactors 7 respectively; The outlet of the reactor top of two breakdown jacket reactors 7 communicates with the import of condenser 8 respectively, and the outlet of condenser communicates with the import of moisture trap 9; Isolated sulfur dioxide gas is sent to liquefaction and is handled, as industrial chemicals;
The reative cell 7-1 of breakdown jacket reactor is connected with the end of tubulation 7-2 and communicates, and discharge bucket 7-3 is connected with the other end of tubulation and communicates, and the smoke inlet that is connected the chuck 7-4 of reative cell and tubulation outside communicates with flue;
The lower end of discharge bucket communicates with centrifuge 10, separates the sodium sulfite solid obtain as the circulation absorbent by centrifuge, turns back in the first absorption liquid circulating slot 2, recycles;
Liquid after the separation continues to decompose again from the outlet of centrifuge turns back to the reative cell 7-1 of breakdown jacket reactor.
Desulfurized step is as follows:
The first step, preparation initial absorption liquid: the initial absorption agent is Na
2CO
3, soft water (deionized water) is added in the first absorption liquid circulating slot 2, under agitation add Na gradually
2CO
3, the weight percent concentration that makes it in solution is 8%, fully after the dissolving, adds solution weight 0.05% antioxidant-p-phenylenediamine (PPD) again, stirs all;
Second step, circulation initial absorption liquid: the circulating pump of opening the first absorption liquid circulating slot 2 and the second absorption liquid circulating slot 3, make absorption liquid spray into the district of going up of desulfurizing tower 1 inside by the first shower nozzle 2-1 that communicates with the first absorption liquid circulating slot, so that absorption sulfur in smoke, then, get back to the first absorption liquid circulating slot from the bottom in this district, the bottom from the first absorption liquid circulating slot flows into the second absorption liquid circulating slot again; Make absorption liquid spray into the middle district of desulfurizing tower 1 inside by the second shower nozzle 3-1 that communicates with the second absorption liquid circulating slot simultaneously, so that absorb sulfur in smoke, then, the second absorption liquid circulating slot is got back in the bottom of distinguishing from this;
The 3rd step, flue gas cool-down: the temperature that flue is discharged be approximately 180 ℃ flue gas respectively from the smoke inlet of two " breakdown jacket reactor " sides enter the chuck and tubulation between carry out heat exchange; Flue gas after temperature descends enters two heat exchangers 6 from the exhanst gas outlet of two " breakdown jacket reactors " respectively and carries out heat exchange once more, the flue gas that reduces once more after the temperature is discharged from the exhanst gas outlet of two heat exchangers, and enters in it from the smoke inlet of washing cooling tower 4 bottoms; Water in the wash water circulating slot 5 sprays from the top of washing in the cooling tower from shower nozzle 5-1 through water pump, further reduces the temperature of flue gas, to below 60 ℃;
The 4th step, absorb sulfur dioxide: the flue gas that temperature is reduced to below 60 ℃ is discharged from the exhanst gas outlet at washing cooling tower 4 tops, enter inferior segment in it from the smoke inlet of desulfurizing tower 1 bottom again, flue gas carries out reasonable distribution in this district, equably from first the shade of each riser at interval enter desulfurizing tower the district, contact the part SO in the flue gas with the absorption liquid of second shower nozzle spray that is located at Zhong Qu top
2Be absorbed; Flue gas enters the district of desulfurizing tower from second the shade of each riser at interval, and is located at the absorption liquid that the first shower nozzle 2-1 that distinguishes top sprays and contacts the remaining SO in the flue gas
2The overwhelming majority is absorbed, and then, enters the chimney discharging from the exhanst gas outlet at desulfurizing tower top; Following chemical reaction takes place:
Na
2CO
3+SO
2＝Na
2SO
3+CO
2↑
Sodium sulfite that obtains with reaction and the SO in the flue gas
2It is as follows to react:
Na
2SO
3+SO
2+H
2O＝2NaHSO
3
The 5th step, decompose sodium hydrogensulfite: the solution of sodium bisulfite that absorption liquid and sulfur in smoke reaction generate, pump into two coiled pipes in the heat exchanger 6 through water pump from the second absorption liquid circulating slot 3, after preheating, enter in the reative cell of two breakdown jacket reactors 7 respectively, reach the flue gas heating between tubulation again in the chuck of breakdown jacket reactor, it is as follows that decomposition reaction takes place:
2NaHSO
3→Na
2SO
3+SO
2↑+H
2O
In the 6th step, separate the sulfur dioxide in the steam: the 5th step was decomposed the SO that generates
2Discharge from the reative cell outlet at breakdown jacket reactor top, enter condenser 8 coolings again, make SO
2Most of water vapor condensation in the gas is a water, then, discharges from the outlet of condenser, enters moisture trap 9, carry out gas-water separation after, with SO
2Gas is sent to liquefaction and is handled, as industrial chemicals;
In the 7th step, recycling sodium sulfite: the 5th step was decomposed the Na that generates
2SO
3And H
2O is discharged into centrifuge 10 from the discharge bucket 7-3 of breakdown jacket reactor bottom to be separated; The centrifuge separation is obtained Na
2SO
3Solid add in the first absorption liquid circulating slot 2 recycling in addition as the circulation absorbent;
In the 8th step, separating filtrate is handled: contain NaHSO in the 7th filtrate that goes on foot under taking advantage of
3, Na
2SO
3And Na
2SO
4, pump into again in the reative cell of breakdown jacket reactor 7, make NaHSO wherein
3Decompose; Na in separating filtrate
2SO
4Content reach at 5% o'clock, separating filtrate is sent to freezing and crystallizing, isolate byproduct Na
2SO
4
Embodiment two: sodium carbonate is adopted in the initial absorption agent, by energy-saving type sodium sulphite circulation desulfurizing device flue gas is carried out desulfurization and handles.
The first step, preparation initial absorption liquid: the initial absorption agent is Na
2CO
3, soft water (deionized water) is added in the first absorption liquid circulating slot 2, under agitation add Na gradually
2CO
3, the weight percent concentration that makes it in solution is 16%, fully after the dissolving, adds solution weight 0.05% antioxidant-p-phenylenediamine (PPD) again, stirs all; All the other steps are identical with embodiment one.
Embodiment three: sodium carbonate is adopted in the initial absorption agent, by energy-saving type sodium sulphite circulation desulfurizing device flue gas is carried out desulfurization and handles.
The first step, preparation initial absorption liquid: the initial absorption agent is Na
2CO
3, soft water (deionized water) is added in the first absorption liquid circulating slot 2, under agitation add Na gradually
2CO
3, the weight percent concentration that makes it in solution is 18%, fully after the dissolving, adds solution weight 0.05% antioxidant-hydroquinones again, stirs all; All the other steps are identical with embodiment one.
Embodiment four: NaOH is adopted in the initial absorption agent, by energy-saving type sodium sulphite circulation desulfurizing device flue gas is carried out desulfurization and handles.
The first step, preparation initial absorption liquid: the initial absorption agent is NaOH, soft water (deionized water) is added in the first absorption liquid circulating slot 2, under agitation add NaOH gradually, make it weight percent concentration in solution and be 7% fully after the dissolving, be adjusted to the saturated solution under the room temperature, add solution weight 0.05% antioxidant-p-phenylenediamine (PPD) again, stir all; Following chemical reaction takes place:
2NaOH+SO
2→Na
2SO
3+H
2O
Sodium sulfite that obtains with reaction and the SO in the flue gas
2It is as follows to react:
Na
2SO
3+SO
2+H
2O＝2NaHSO
3
All the other steps are identical with embodiment one.
Embodiment five: NaOH is adopted in the initial absorption agent, by energy-saving type sodium sulphite circulation desulfurizing device flue gas is carried out desulfurization and handles.
The first step, preparation initial absorption liquid: the initial absorption agent is NaOH, soft water (deionized water) is added in the first absorption liquid circulating slot 2, under agitation add NaOH gradually, the weight percent concentration that makes it in solution is 12.5%, fully after the dissolving, add solution weight 0.05% antioxidant-p-phenylenediamine (PPD) again, stir all; Following chemical reaction takes place:
2NaOH+SO
2→Na
2SO
3+H
2O
The sodium sulfite that obtains with reaction is as the SO in circulation absorbent and the flue gas
2It is as follows to react:
Na
2SO
3+SO
2+H
2O＝2NaHSO
3
All the other steps are identical with embodiment one.
Embodiment six: NaOH is adopted in the initial absorption agent, by energy-saving type sodium sulphite circulation desulfurizing device flue gas is carried out desulfurization and handles.
The first step, preparation initial absorption liquid: the initial absorption agent is NaOH, soft water (deionized water) is added in the first absorption liquid circulating slot 2, under agitation add NaOH gradually, the weight percent concentration that makes it in solution is 14%, fully after the dissolving, add solution weight 0.05% antioxidant one hydroquinones again, stir all; Following chemical reaction takes place:
2NaOH+SO
2→Na
2SO
3+H
2O
Sodium sulfite that obtains with reaction and the SO in the flue gas
2It is as follows to react:
Na
2SO
3+SO
2+H
2O＝2NaHSO
3
All the other steps are identical with embodiment one.
The present invention can be according to what of actual exhaust gas volumn, can use a heat exchanger and breakdown jacket reactor or many heat exchangers and Duo Tai breakdown jacket reactor, can derive a plurality of embodiment from above embodiment, do not enumerate one by one.
Claims (7)
1. energy-saving type sodium sulphite circulation desulfurizing device comprises desulfurizing tower (1), is located at the desulfurizing tower outer first absorption liquid circulating slot (2) and the second absorption liquid circulating slot (3), and the inside of desulfurizing tower is divided into three districts, upper, middle and lower at interval by twice; The district is provided with first shower nozzle (2-1) that communicates with the first absorption liquid circulating slot on desulfurizing tower inside, and bottom in district communicates with the first absorption liquid circulating slot on this; Be provided with second shower nozzle (3-1) that communicates with the second absorption liquid circulating slot in the middle district of desulfurizing tower inside, the bottom of distinguishing in this communicates with the second absorption liquid circulating slot; The bottom of the first absorption liquid circulating slot communicates with the second absorption liquid circulating slot; The exhanst gas outlet at desulfurizing tower top communicates with chimney, the smoke inlet of desulfurizing tower bottom communicates with the exhanst gas outlet at washing cooling tower (4) top, the bottom of washing cooling tower communicates with recirculated water washing trough (5), and the 3rd shower nozzle (5-1) that communicates with the recirculated water washing trough is located at the top in the washing cooling tower; It is characterized in that:
The smoke inlet of a, washing cooling tower (4) bottom communicates with the exhanst gas outlet of a heat exchanger (6) bottom at least, the smoke inlet on heat exchanger top communicates with the exhanst gas outlet of breakdown jacket reactor (7) side, and the smoke inlet of breakdown jacket reactor side communicates with flue;
Coiled pipe in the outlet of b, second absorption liquid circulating slot (3) bottom and the heat exchanger (6) communicates, and the outlet of coiled pipe communicates with the reative cell of breakdown jacket reactor (7); The outlet of the reactor top of breakdown jacket reactor (7) communicates with the import of condenser (8), and the outlet of condenser communicates with the import of moisture trap (9);
The bottom of c, breakdown jacket reactor (7) communicates with a desk centrifuge (10), and the outlet of centrifuge communicates with the reative cell of breakdown jacket reactor (7).
2. energy-saving type sodium sulphite circulation desulfurizing device according to claim 1 is characterized in that: described breakdown jacket reactor (7) comprises the tubulation (7-2) that reative cell (7-1), an end be connected with reative cell, the discharge bucket (7-3) that is connected with the other end of tubulation, the chuck (7-4) that is connected reative cell and tubulation side; Smoke inlet on the chuck communicates with flue, and the lower end of discharge bucket communicates with centrifuge (10).
3. energy-saving type sodium sulphite circulation desulfurizing device according to claim 1 and 2, it is characterized in that: the smoke inlet of washing cooling tower (4) bottom communicates with the exhanst gas outlet of two heat exchangers (6) bottom, the smoke inlet on two heat exchanger tops communicates with the exhanst gas outlet of two breakdown jacket reactors (7) side respectively, and the smoke inlet of two breakdown jacket reactor bottoms communicates with flue respectively;
The outlet of second absorption liquid circulating slot (3) bottom respectively with two heat exchangers (6) in coiled pipe (6-1) communicate, the outlet of two coiled pipes communicates with the reative cell of two breakdown jacket reactors (7) respectively; The outlet of the reactor top of two breakdown jacket reactors (7) communicates with the import of condenser (8) respectively, and the outlet of condenser communicates with the import of moisture trap (9);
The discharge bucket (7-3) of the bottom of two breakdown jacket reactors (7) communicates with a desk centrifuge (10) respectively, and the outlet of two desk centrifuges communicates with the reative cell (7-1) of two breakdown jacket reactors (7) respectively.
4. energy-saving type sodium sulphite circulation desulfurization method is carried out on the described energy-saving type sodium sulphite circulation desulfurizing device of claim 1, and its step is as follows:
The first step, preparation initial absorption liquid: the initial absorption agent is Na
2CO
3, soft water is added in the first absorption liquid circulating slot (2), under agitation add Na gradually
2CO
3, the weight percent concentration that makes it in solution is 8-18%, fully after the dissolving, adds solution weight 0.05% antioxidant again, stirs all;
Second step, circulation initial absorption liquid: the circulating pump of opening the first absorption liquid circulating slot (2) and the second absorption liquid circulating slot (3), making absorption liquid spray into inner the going up of desulfurizing tower (1) by first shower nozzle (2-1) that communicates with the first absorption liquid circulating slot distinguishes, get back to the first absorption liquid circulating slot from the bottom in this district again, flow into the second absorption liquid circulating slot from the bottom of the first absorption liquid circulating slot; Make absorption liquid spray into the inner middle district of desulfurizing tower (1) by second shower nozzle (3-1) that communicates with the second absorption liquid circulating slot simultaneously, the second absorption liquid circulating slot is got back in the bottom of distinguishing from this again;
The 3rd step, flue gas cool-down: the temperature that flue is discharged be approximately 180 ℃ flue gas from the smoke inlet of " breakdown jacket reactor " side enter the chuck and tubulation between carry out heat exchange; Flue gas after temperature descends enters heat exchanger (6) from the exhanst gas outlet of " breakdown jacket reactor " and carries out heat exchange once more, the flue gas that reduces once more after the temperature is discharged from the exhanst gas outlet of heat exchanger, and enters in it from the smoke inlet of washing cooling tower (4) bottom; Water in the wash water circulating slot (5) sprays from the top of washing in the cooling tower from shower nozzle (5-1) through water pump, further reduces the temperature of flue gas, to below 60 ℃;
The 4th step, absorb sulfur dioxide: the flue gas that temperature is reduced to below 60 ℃ is discharged from the exhanst gas outlet at washing cooling tower (4) top, smoke inlet from desulfurizing tower (1) bottom enters its interior inferior segment again, flue gas carries out reasonable distribution in this district, equably from first the shade of riser at interval enter desulfurizing tower the district, contact the part SO in the flue gas with the absorption liquid of second shower nozzle (3-1) spray that is located at Zhong Qu top
2Be absorbed; Flue gas enters the district of desulfurizing tower from second the shade of riser at interval, and is located at the absorption liquid that first shower nozzle (2-1) of distinguishing top sprays and contacts the remaining SO in the flue gas
2The overwhelming majority is absorbed, and then, enters the chimney discharging from the exhanst gas outlet at desulfurizing tower top; Following chemical reaction takes place:
Na
2CO
3+SO
2＝Na
2SO
3+CO
2↑
Sodium sulfite that obtains with reaction and the SO in the flue gas
2It is as follows to react:
Na
2SO
3+SO
2+H
2O＝2NaHSO
3
The 5th step, decompose sodium hydrogensulfite: the solution of sodium bisulfite that absorption liquid and sulfur in smoke reaction generate, pump into coiled pipe in the heat exchanger (6) through water pump from the second absorption liquid circulating slot (3), after preheating, enter in the reative cell of breakdown jacket reactor (7), in the chuck of breakdown jacket reactor (7), reach the flue gas heating between tubulation again, take place to decompose as follows:
2NaHSO
3→Na
2SO
3+SO
2↑+H
2O
In the 6th step, separate the sulfur dioxide in the steam: the 5th step was decomposed the SO that generates
2Discharge from the reative cell outlet at breakdown jacket reactor top, enter condenser (8) cooling again, make SO
2Most of water vapor condensation in the gas is a water, then, discharges from the outlet of condenser, enters moisture trap (9), carry out gas-water separation after, with SO
2Gas is sent to liquefaction and is handled, as industrial chemicals;
In the 7th step, recycling sodium sulfite: the 5th step was decomposed the Na that generates
2SO
3And H
2O is discharged into centrifuge (10) from the discharge bucket (7-3) of breakdown jacket reactor bottom to be separated; The centrifuge separation is obtained Na
2SO
3Solid to add the first absorption liquid circulating slot (2) recycling;
In the 8th step, separating filtrate is handled: contain NaHSO in the 7th filtrate that goes on foot under taking advantage of
3, Na
2SO
3And Na
2SO
4, pump into again in the reative cell of breakdown jacket reactor (7), make NaHSO wherein
3Decompose; Na in separating filtrate
2SO
4Content reach at 5% o'clock, separating filtrate is sent to freezing and crystallizing, isolate byproduct Na
2SO
4
5. energy-saving type sodium sulphite circulation desulfurization method according to claim 4, it is characterized in that: the first step, preparation initial absorption liquid: the initial absorption agent is NaOH, soft water is added in the first absorption liquid circulating slot (2), under agitation add NaOH gradually, the weight percent concentration that makes it in solution is 7-14%, fully after the dissolving, add solution weight 0.05% antioxidant again, stir all; Following chemical reaction takes place:
2NaOH+SO
2→Na
2SO
3+H
2O
Sodium sulfite that obtains with reaction and the SO in the flue gas
2It is as follows to react:
Na
2SO
3+SO
2+H
2O＝2NaHSO
3
6. according to claim 4 or 5 described energy-saving type sodium sulphite circulation desulfurization methods, it is characterized in that: the antioxidant that adds in the absorption liquid is p-phenylenediamine (PPD) or hydroquinones.
7. according to claim 4 or 5 described energy-saving type sodium sulphite circulation desulfurization methods, it is characterized in that: when the circulation absorbent after loss appears in desulfurization, need in time to replenish initial absorption agent Na
2CO
3, or NaOH.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007100782507A CN101254392B (en) | 2007-02-28 | 2007-02-28 | Energy-saving sodium sulfite circulating desulfurization device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2007100782507A CN101254392B (en) | 2007-02-28 | 2007-02-28 | Energy-saving sodium sulfite circulating desulfurization device and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101254392A true CN101254392A (en) | 2008-09-03 |
| CN101254392B CN101254392B (en) | 2011-01-12 |
Family
ID=39889699
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2007100782507A Expired - Fee Related CN101254392B (en) | 2007-02-28 | 2007-02-28 | Energy-saving sodium sulfite circulating desulfurization device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101254392B (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101444699B (en) * | 2008-12-16 | 2011-04-13 | 刘存宝 | Technical method for removing sulfur dioxide in flue gas by using sodium sulfite and equipment thereof |
| CN103303945A (en) * | 2013-06-30 | 2013-09-18 | 金川集团股份有限公司 | Vapor recovery system and method for sodium sulfite evaporation and concentration process |
| CN103657341A (en) * | 2013-12-10 | 2014-03-26 | 陕西省石油化工研究设计院 | An anti-oxidation type SO2 absorption recovery agent |
| CN105056744A (en) * | 2015-09-20 | 2015-11-18 | 山西长林环保机械设备有限公司 | Flue gas waste heat recovery and desulfurization integrated process and device |
| CN106000048A (en) * | 2016-06-20 | 2016-10-12 | 广东上典环境保护工程有限公司 | Low-temperature desulfuration and denitration system |
| CN106219573A (en) * | 2016-08-26 | 2016-12-14 | 海洲环保集团有限公司 | A kind of except scar salt production system |
| CN108654334A (en) * | 2018-06-20 | 2018-10-16 | 芜湖盛科环保技术有限公司 | A kind of high temperature sulfur-containing smoke gas Special filtering device |
| CN109316936A (en) * | 2018-11-06 | 2019-02-12 | 张锐 | A kind of agricultural soil reparation incineration method flue gas purification device |
| CN112933907A (en) * | 2021-02-08 | 2021-06-11 | 上海交通大学 | System and method for wet absorption, regeneration and recovery of sulfur dioxide |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5573325A (en) | 1978-11-27 | 1980-06-03 | Toray Ind Inc | Separation of sulfur dioxide gas from exhaust gas |
| JP3741400B2 (en) | 1998-03-06 | 2006-02-01 | 月島機械株式会社 | Exhaust gas desulfurization method and apparatus |
| CN2640584Y (en) * | 2003-09-17 | 2004-09-15 | 镇江市江南环保设备研究所 | Integrated equipment for desulfurizing and discharging smoke |
| CN1283346C (en) * | 2003-09-17 | 2006-11-08 | 镇江市江南环保设备研究所 | Fuel coal smoke low oxidation rate desulfur method |
| CN2822758Y (en) * | 2005-07-04 | 2006-10-04 | 向瑞先 | Sectional jacketed-type reactor |
-
2007
- 2007-02-28 CN CN2007100782507A patent/CN101254392B/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101444699B (en) * | 2008-12-16 | 2011-04-13 | 刘存宝 | Technical method for removing sulfur dioxide in flue gas by using sodium sulfite and equipment thereof |
| CN103303945A (en) * | 2013-06-30 | 2013-09-18 | 金川集团股份有限公司 | Vapor recovery system and method for sodium sulfite evaporation and concentration process |
| CN103657341A (en) * | 2013-12-10 | 2014-03-26 | 陕西省石油化工研究设计院 | An anti-oxidation type SO2 absorption recovery agent |
| CN103657341B (en) * | 2013-12-10 | 2016-04-06 | 陕西省石油化工研究设计院 | A kind of anti-oxidative SO 2absorb recovery catalyst |
| CN105056744A (en) * | 2015-09-20 | 2015-11-18 | 山西长林环保机械设备有限公司 | Flue gas waste heat recovery and desulfurization integrated process and device |
| CN105056744B (en) * | 2015-09-20 | 2017-09-12 | 山西长林能源科技有限公司 | A kind of flue gas waste heat recovery, desulfurization integrated technique and device |
| CN106000048A (en) * | 2016-06-20 | 2016-10-12 | 广东上典环境保护工程有限公司 | Low-temperature desulfuration and denitration system |
| CN106000048B (en) * | 2016-06-20 | 2018-06-12 | 广东上典环境保护工程有限公司 | A kind of low-temp desulfurization and denitrating system |
| CN106219573A (en) * | 2016-08-26 | 2016-12-14 | 海洲环保集团有限公司 | A kind of except scar salt production system |
| CN108654334A (en) * | 2018-06-20 | 2018-10-16 | 芜湖盛科环保技术有限公司 | A kind of high temperature sulfur-containing smoke gas Special filtering device |
| CN109316936A (en) * | 2018-11-06 | 2019-02-12 | 张锐 | A kind of agricultural soil reparation incineration method flue gas purification device |
| CN112933907A (en) * | 2021-02-08 | 2021-06-11 | 上海交通大学 | System and method for wet absorption, regeneration and recovery of sulfur dioxide |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101254392B (en) | 2011-01-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN200998639Y (en) | Concentrated crystallization and absorbed oxidation combined type ammonia process desulfuration tower | |
| CN101254392A (en) | Energy-saving type sodium sulphite circulation desulfurizing device and method | |
| EA029429B1 (en) | Method for treating flue gas and apparatus for treating acidic tail gas by using ammonia process | |
| CN203108424U (en) | Flue gas treatment apparatus performing desulfurization and denitrification simultaneously | |
| CN201324593Y (en) | Wet ammonia flue gas desulphurization device | |
| CN101073741A (en) | Method and apparatus for combined removing sulfur-dioxide and nitrogenoxide by mixed solution | |
| CN201026440Y (en) | Absorption, oxidation, concentration combined desulfurizing tower | |
| CN101890281A (en) | Forward flow and backward flow combined spray desulfurizing tower | |
| CN103977664B (en) | A kind of method of flue gas desulfurization denitration dust-removing | |
| CN103463910A (en) | Comprehensive treatment device and method for cooling desulfurization of high-temperature and high-humidity flue gas | |
| CN102614768B (en) | Desulfurization reactor device | |
| CN201510842U (en) | Double-loop hollow tower spray and tower body demisting air flue integrating device | |
| CN102210967A (en) | Two-stage treatment wet desulphurization method for high-sulfur coal-fired flue gas | |
| CN209501361U (en) | Novel energy-conserving Complexing Iron desulphurization plant | |
| CN104226102B (en) | A kind of aluminium electrolytic flue horizontal spraying desulfurizer and method | |
| CN1660474A (en) | Wet flue gas desulfurization process | |
| CN104971597A (en) | Technical method and device of producing sodium hydrosulfide from acid gas | |
| TWI633923B (en) | Method and device for processing acid gas | |
| CN203507740U (en) | Cooling and desulfurizing comprehensive treatment device of high-temperature and high-humidity flue gas | |
| CN205570080U (en) | Coke oven smoke desulfurization system | |
| CN101439258A (en) | High-efficiency synthetic desulphurization technique without waste liquid | |
| CN101143293B (en) | Method for deodorant waste lye for absorbing treating smoke | |
| CN204107322U (en) | A kind of aluminium electrolytic flue horizontal spraying desulfurizer | |
| CN107261789A (en) | The ammonia method desulfurizing system and method for a kind of high-sulfur flue gas | |
| CN207581563U (en) | A kind of novel ammonia water circulation desulfurization system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110112 Termination date: 20120228 |