CN105056746A - Method for realizing boiler flue gas integrated distributed desulfurization and denitrification process - Google Patents
Method for realizing boiler flue gas integrated distributed desulfurization and denitrification process Download PDFInfo
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- CN105056746A CN105056746A CN201510506429.2A CN201510506429A CN105056746A CN 105056746 A CN105056746 A CN 105056746A CN 201510506429 A CN201510506429 A CN 201510506429A CN 105056746 A CN105056746 A CN 105056746A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 239000003546 flue gas Substances 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 47
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 30
- 230000008569 process Effects 0.000 title claims abstract description 20
- 230000023556 desulfurization Effects 0.000 title abstract description 19
- 239000002002 slurry Substances 0.000 claims abstract description 45
- 230000001590 oxidative effect Effects 0.000 claims abstract description 30
- 230000003647 oxidation Effects 0.000 claims abstract description 26
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 26
- 238000005507 spraying Methods 0.000 claims abstract description 19
- 239000007921 spray Substances 0.000 claims description 36
- 230000003009 desulfurizing effect Effects 0.000 claims description 28
- 239000007788 liquid Substances 0.000 claims description 14
- 239000000779 smoke Substances 0.000 claims description 14
- 238000010521 absorption reaction Methods 0.000 claims description 13
- 239000002250 absorbent Substances 0.000 claims description 12
- 230000002745 absorbent Effects 0.000 claims description 12
- 239000007800 oxidant agent Substances 0.000 claims description 12
- 230000000694 effects Effects 0.000 claims description 10
- 230000010354 integration Effects 0.000 claims description 7
- 238000000746 purification Methods 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 6
- 230000008859 change Effects 0.000 claims description 5
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 4
- 239000010962 carbon steel Substances 0.000 claims description 4
- 239000011521 glass Substances 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 241000628997 Flos Species 0.000 claims description 3
- 239000011152 fibreglass Substances 0.000 claims description 3
- 239000011800 void material Substances 0.000 claims description 3
- 239000000428 dust Substances 0.000 abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 39
- 239000000243 solution Substances 0.000 description 15
- 238000005516 engineering process Methods 0.000 description 13
- 238000013461 design Methods 0.000 description 8
- 239000007789 gas Substances 0.000 description 8
- 239000003513 alkali Substances 0.000 description 7
- 230000008901 benefit Effects 0.000 description 7
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical group [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 239000010440 gypsum Substances 0.000 description 3
- 229910052602 gypsum Inorganic materials 0.000 description 3
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 230000035800 maturation Effects 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 241000521257 Hydrops Species 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 206010030113 Oedema Diseases 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 230000003044 adaptive effect Effects 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- -1 and after reaction Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000005094 computer simulation Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010369 molecular cloning Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 150000003463 sulfur Chemical class 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Treating Waste Gases (AREA)
Abstract
The invention relates to a method for realizing an integrated distributed desulfurization and denitrification process of boiler flue gas, which is characterized by comprising the following steps of: the method comprises the following steps: firstly, flue gas enters a desulfurization tower from the lower part after passing through a dust remover, slurry in a slurry pool is conveyed to a nozzle at the upper part of the desulfurization tower through a circulating pump for spraying, and the purified flue gas enters an oxidation tower after being demisted by a demister; secondly, the flue gas enters the oxidation tower from the top, the slurry in the slurry pool is conveyed to a nozzle at the upper part of the oxidation tower through a circulating pump for spraying, and the oxidized flue gas enters the denitrification tower after passing through a wire mesh demister; step three, the flue gas enters the denitration tower from the lower part, 3 layers of spraying are arranged in the tower, the slurry in the first layer and the slurry in the third layer are conveyed to a nozzle in the lower layer for spraying through a circulating pump, and the slurry in the second layer is externally connected with H2O2And spraying the solution to achieve the process of absorbing firstly, oxidizing and then absorbing, wherein the purified flue gas is demisted by a demister above the denitration tower and then discharged by a chimney.
Description
Technical field
The present invention relates to field of Environment Protection, relate to a kind of coal-burning boiler discharge the purification method of flue gas, specifically refer to the implementation method of the distributed desulfurizing and denitrifying process of a kind of boiler smoke integration.
Background technology
Along with China's expanding economy, China increases significantly to the demand of the energy and consumption, a large amount of fossil fuels discharges the pollutants such as SO2, NOx, dust in combustion and brings serious environmental problem, also promote fuel, the particularly research and development of the clean combustion technique of coal, wherein coal-fired sulfur dioxide and Emission Controlling Technology of Nitric Oxides are the hot subjects studied in the world in the last few years.At present, most or stand-alone development for technology and equipments such as coal burning flue gas desulfurization, denitration and flue gas ash removals, form respective technical system and technological process, for realizing the respective requirement to desulphurization and denitration, need to build many covering devices, complex process, investment larger.
Current desulphurization denitration technology is all concentrate in a tower to carry out, and gas denitrifying technology mainly contains SCR (SCR) and SNCR (SNCR), is all utilize ammonia to make reducing agent, and the product of reduction is nitrogen.Wherein SCR method denitration efficiency is high, but its technology and equipment system is more complicated, and expensive catalyst, consumption are large, and plant running cost is high; SNCR method technology and equipment system is comparatively simple, and plant running cost is not high, but denitration rate can not ensure.The more employing of flue gas desulfurization be limestone-gypsum method, the investment of this sulfur method is comparatively large, consume a large amount of limestone resources, and produces desulfurization wastewater and a large amount of gypsum of by-product, and by-product is worth not high.Along with the extensive use of ammonia-process desulfurization technique, the advantage of the ammonia process of desulfurization manifests day by day.The ammonia process of desulfurization can the valuable product such as producing ammonium sulfate byproduct chemical fertilizer while desulfurization, and does not produce any secondary pollution, belongs to the desulfur technology of green clean complete resource.But its denitration ability is not high.
Summary of the invention
Technical problem to be solved by this invention is the implementation method providing the distributed desulfurizing and denitrifying process of a kind of boiler smoke integration for above-mentioned prior art, the method of dedusting-desulfurization-oxidation-denitration is adopted to carry out fume treatment, while its denitrification efficiency of raising, reduce the operating cost of device.
The present invention's adopted technical scheme that solves the problem is: the implementation method of the distributed desulfurizing and denitrifying process of a kind of boiler smoke integration, carry out in system for desulfuration and denitration, this system comprises deduster, desulfurizing tower, oxidizing tower, denitrating tower and slurry pool, said method comprising the steps of:
Step one, flue gas enter desulfurizing tower from below after deduster, slurries in slurry pool are transported to the nozzle spray on desulfurizing tower top by circulating pump, in stock tank, slurries form containing the configuration of 5-20% mass percent alkaline absorbent, there is strong blending and effect of mass transmitting in slurries and flue gas, reaches and remove SO
2effect, the flue gas after purification, enters oxidizing tower after the demister demist above desulfurizing tower;
Step 2, flue gas enter oxidizing tower from top, slurries in slurry pool are transported to the nozzle spray on oxidizing tower top by circulating pump, in stock tank, slurries form containing the configuration of 5-20% mass percent oxidant, there is strong blending and effect of mass transmitting in slurries and flue gas, reach the effect of oxidation NO, flue gas after oxidation, enters denitrification column after the wire mesh demister in the floss hole offered below oxidizing tower side;
Step 3, flue gas enter denitrating tower from bottom, and have three layers in tower spray, and ground floor slurries are the alkaline absorbent solution in slurry pool, are transported to underlying nozzle spray by circulating pump, and second layer spray is external H
2o
2solution spraying, third layer slurries are the alkaline absorbent solution in slurry pool, and be delivered to upper strata nozzle spray by circulating pump, reach and first absorb the resorbent process of rear oxidation, the flue gas after purification, by smoke stack emission after the demister demist above denitrating tower.
Be void tower structure in described desulfurizing tower, material is warm glass flake in carbon steel lining, is provided with two-layer spraying layer in tower, and spraying layer adopts glass reinforced plastic pipe and nozzle, and the gas-liquid contact mode of employing is the mode of reverse spray.
In order to adapt to the change of flue-gas temperature completely, pre-cooled device being set before desulfurizing tower entrance, guaranteeing that the temperature that flue gas enters absorption tower is less than 120 DEG C.
Compared with prior art, the invention has the advantages that:
The first desulfurization of the present invention avoids oxidant SO
3 2-be oxidized to SO
4 2-, desulfurization rear oxidation by the NO that absorbent absorbs, is not oxidized to NO
2.Absorb again after oxidation, because 3 molecule NO
2the NO of a molecule can be generated after absorption, be therefore oxidized again, absorb, reach the object of qualified discharge.The present invention adopts suitable oxidant in oxidation on suitable opportunity, and save oxidant, the amount that can be sprayed into by secondary oxidation agent controls nitrogen oxide exit concentration, and 3 times spray Alkali absorption also can lower SO
2concentration of emission, therefore can adapt to different operating mode, different pollutant levels, while its denitrification efficiency of raising, reduce the operating cost of device.
Accompanying drawing explanation
Fig. 1 is the system for desulfuration and denitration structural representation in the embodiment of the present invention.
Deduster 1, desulfurizing tower 2, oxidizing tower 3, denitrating tower 4, air-introduced machine 5, circulating pump 6, demister 7, efflux pump 8, absorbent alkali adding tank 9, measuring pump 10, slurry pool 11, flue 12, wire mesh demister 13, H
2o
2naOH solution tank NaOH 14, oxidant alkali adding tank 15.
Detailed description of the invention
Below in conjunction with accompanying drawing embodiment, the present invention is described in further detail.
As shown in Figure 1, the implementation method of the distributed desulfurizing and denitrifying process of a kind of boiler smoke integration in the present embodiment, adopt the route of dedusting-desulfurization-oxidation-denitration, what dedusting adopted is sack cleaner 1; Enter desulfurizing tower 2 again, desulfurizing tower 2 adopts the mode of packed tower, and absorbent is dilute solution of sodium hydroxide; Then enter oxidizing tower 3 and carry out once oxidation absorption, a part of NO is oxidized to NO
2, adopt the mode along spray in oxidizing tower 3, the flue gas after once oxidation enters denitrating tower 4 subsequently and carries out double absorption oxidation, and most of NO is oxidized to NO
2and absorb, adopt the mode of packed tower.Once oxidation oxidant is NaClO, and secondary oxidation oxidant is H
2o
2.
The method that in this programme, desulfurization adopts is NaOH alkali absorption method, and other alkaline solutions also can carry out desulfurization process as absorbent, and dilute solution of sodium hydroxide is as the SO in absorbent and flue gas
2reaction, the gas-liquid contact mode adopted is the mode of reverse spray, namely flue gas is entered by bottom desulfurizing tower by air-introduced machine 5 after deduster 1, sodium hydroxide slurry below tower in stock tank is delivered to upper nozzle spray by circulating pump 6, spray liquid is sprayed to fall to forming reversed hedge with flue gas by top, contact area and the time of contact of flue gas and spray liquid can be improved, thus raising desulfuration efficiency, in stock tank, slurries form containing the configuration of 5-20% mass percent NaOH, there is strong blending and effect of mass transmitting in slurries and flue gas, reaches and remove SO
2effect, the flue gas after purification, enters oxidizing tower 2 after demister 7 demist.Be void tower structure in desulfurizing tower, material is warm glass flake in carbon steel lining, two-layer spraying layer.Spraying layer adopts glass reinforced plastic pipe+nozzle, prevent from rotting and blocking, whole tower body effective cross section (smoke distribution cross section) is sufficiently and reasonably covered, gas liquid interfacial area and contact probability large, effective raising desulfuration efficiency, reach best gas-liquid contact and detersive efficiency, thus realize the highest desulfuration efficiency.Spray liquid flows into reaction tank after falling at the bottom of tower, and control caustic dosage and efflux wastewater amount by pH value, waste liquid is discharged by efflux pump 8, and outside NaOH alkali adding tank 9 controls to join in slurry pool 11 by measuring pump 10.The accessory substance generated is Na
2sO
3, NaHSO
3solution, qualified discharge after being regulated by PH.In order to adapt to the change of flue-gas temperature completely, pre-cooled device being set before desulfurizing tower entrance, guaranteeing that the temperature that flue gas enters absorption tower is less than 120 DEG C.Desulfurization principle is as follows:
SO
2+2NaOH→Na
2SO
3+H
2O
Na
2SO
3+SO
2+H
2O→2NaHSO
3
(1) run conveniently, use with the opening, with Guan Suiting.
(2) desulfuration efficiency is high.Desulfurization degree is up to more than 96%, and the flue gas after desulfurization not only sulfur dioxide concentration is very low, and dust content also greatly reduces.
(3) technology maturation, operational reliability is high.External lime stone-gypsum desulfurizer operational percentage generally reaches more than 98%, because its developing history length, technology maturation, operating experience are many, therefore can not affect sintering circuit because of desulphurization plant and normally run, can ensure running time in desulfurizer year.
(4) system adaptive is strong, completely suitable flue gas flow and SO
2the change of content.Absorption tower spraying layer adopts unit style design, all arranges dedicated pump, according to the opening and closing of flue gas actual state adjustment spraying layer, can be issued to design desulfuration efficiency in minimum energy consumption.In order to the change of completely suitable flue-gas temperature, pre-cooled device is set before desulfurizing tower entrance, guarantees that the temperature that flue gas enters absorption tower is less than 120 DEG C.
(5) desulfuration absorbing tower field fabrication, carbon steel glass inner-lining scale anticorrosion.Taking outside normal anti-corrosion measure, designing for many years according to my company, constructing and system cloud gray model experience, special reinforcement process that is wear-resisting, resistance to erosion is also taked in operation areas different in absorption tower.
(6) pass through to adopt CFD Numeric simulation design, preferentially carry out the connection design of the equipment such as flue, desulfurizing tower, implement flue gas flow equalizing, steady flow, Reaction time shorten, reduction desulfurizing tower resistance while guarantee desulfurization degree.
(7) the slurry nozzle pattern of spraying layer adopts nozzle, and pass through computer simulation, be optimized layout, whole tower body effective cross section (smoke distribution cross section) is sufficiently and reasonably covered, gas liquid interfacial area and contact probability large, effective raising desulfuration efficiency, reaches best gas-liquid contact and detersive efficiency, thus realizes the highest desulfuration efficiency.
(8) adopt empty nozzle, to spray taper liquid film gas liquid contacting efficiency high, without fouling, without precipitation blocking.Nozzle material is SiC, wear-resistant, corrosion-resistant.
(9) system pressure drop is low.
(10) wet sprinkling tower flue gas Treatment process is except having the general advantage of wet sprinkling tower desulfur technology, also has outstanding incomparable technical advantage.
(11) flue gas high-speed cruising
Tested by stage, shown that gas speed is on the impact of absorption tower design, when the empty tower gas velocity of flue gas is up to 4.0m/s, systematic operation still can meet SO
2remove requirement, test also demonstrates removes SO
2with the design equation of pressure drop.The advantage of high velocity smoke stream is to enhance quality transmission capacity, reduces design cost.
(12) optimum tower body size design
Independently investigate reaction zone height to the impact designed a model, under similar reaction zone conditions, determined optimum tower body size: the distance between smoke inlet to the distance, spraying layer of the first spraying layer, system adopt optimum tower body size, balance and remove SO
2with the relation of pressure drop, fund input and operating cost are down to minimum.
In this programme, oxidation technology is as follows: flue gas enters oxidizing tower from top, adopt the mode along spray, NaClO solution is oxidant, by circulating pump, the NaClO solution in pond is delivered to top spray spout, flue gas forward contacts with NaClO solution, and after reaction, reactant liquor falls at the bottom of pond, reactor side opening flue 12, flue gas with at the bottom of reactant liquor to pond after be separated because flue gas turns to, the wire mesh demister 13 through side floss hole carries out degree of depth separation.Control chemical feeding quantity by the pH value of reactant liquor, control efflux wastewater by the cumulant of entrance NO, outside NaClO alkali adding tank 15 controls to join in slurry pool 11 by measuring pump 10.Flue gas through peroxidating laggard enter denitrification column.Solution in stock tank forms containing the configuration of 5-20% mass percent clorox, and strong blending and effect of mass transmitting occur for slurries and flue gas, reach the effect of oxidation NO, and the flue gas after oxidation, enters denitrification column after wire mesh demister.Oxidation mechanisms:
NaClO+H
+→Na
++HClO
HClO+NO→NO
2+HCl
HClO easily decomposes when temperature height, therefore must to the system of keeping under strict control of medium in oxidizing tower.The mode of what this oxidation technology was taked the is outer serum recycle of tower, two-layer spray, adopts wire mesh demister interception molecule when flue gas goes out tower.
Technological advantage:
(1) adopt the mode of reverse spray, flue gas flow rate is than very fast, and air speed can reach 5m/s, and tower diameter is little.
(2) flue gas from the top to the bottom, then draw from the side, and the drop in flue gas is fallen in tower in hydrops due to inertia, reaches the effect of part gas-liquid separation.
(3) control the composition of slurries, avoid the waste of oxidant.
(4) exhanst gas outlet adopts wire mesh demister, can reach the clearance of more than 99%, avoid oxidant to enter in denitrating technique and go the particle of more than 3um.
NaOH weak solution that what the denitrating technique of this technique adopted is as absorbent, NO
2for acidic oxide, very easily by alkali liquor absorption.Flue gas enters denitrating tower bottom from the flue below oxidizing tower side, and have three layers in tower spray, and ground floor NaOH slurries are transported to bottom nozzle spray by circulating pump, and second layer spray is external H
2o
2naOH solution tank NaOH 14 sprays, and third layer NaOH slurries are delivered to upper strata nozzle spray by circulating pump, and three layers of injector spacing are comparatively far away, and reach and first absorb the resorbent process of rear oxidation, the flue gas after purification, by smoke stack emission after demister demist.What adopt is the mode of hollow-spraying-tower, and bottom one deck sprays.Because the NO of 3 molecules
2have one Molecular Cloning for NO, the mode of twice oxidation that what therefore this technique adopted is, sprays H after the lower layer of spray
2o
2solution, carries out secondary oxidation, then carries out second time NaOH solution spray.Spray H can be regulated according to outlet nitrous oxides concentration
2o
2amount.Produce accessory substance NaNO
3, can arrange directly outward.Dewater through wire mesh demister after flue gas washing is clean, last chimney discharging directly into atmosphere.
Denitration principle:
3NO
2+H
2O→2HNO
3+NO
NO+H
2O
2→NO
2+H
2O
HNO
3+NaOH→NaNO
3+H
2O
Technological advantage:
(1) mode of hollow-spraying-tower, flue gas resistance is little.
(2) H is adopted
2o
2as oxidant spray, and reoxidize after once spraying, consumption is relatively little, the unreacted fully reaction that can circulate in slurries.
(3) can according to the concentration adjustment H of exiting flue gas nitrogen oxide
2o
2consumption, adaptation condition ability is stronger.
(4) exhanst gas outlet adopts wire mesh demister, avoids chimney rain phenomenon.
In addition to the implementation, the present invention also includes other embodiments, the technical scheme that all employing equivalents or equivalent substitute mode are formed, within the protection domain that all should fall into the claims in the present invention.
Claims (3)
1. the implementation method of the distributed desulfurizing and denitrifying process of boiler smoke integration, it is characterized in that: carry out in system for desulfuration and denitration, this system comprises deduster (1), desulfurizing tower (2), oxidizing tower (3), denitrating tower (4) and slurry pool (5), said method comprising the steps of:
Step one, flue gas enter desulfurizing tower from below after deduster, slurries in slurry pool are transported to the nozzle spray on desulfurizing tower top by circulating pump, in stock tank, slurries form containing the configuration of 5-20% mass percent alkaline absorbent, there is strong blending and effect of mass transmitting in slurries and flue gas, reaches and remove SO
2effect, the flue gas after purification, enters oxidizing tower after the demister demist above desulfurizing tower;
Step 2, flue gas enter oxidizing tower from top, slurries in slurry pool are transported to the nozzle spray on oxidizing tower top by circulating pump, in stock tank, slurries form containing the configuration of 5-20% mass percent oxidant, there is strong blending and effect of mass transmitting in slurries and flue gas, reach the effect of oxidation NO, flue gas after oxidation, enters denitrification column after the wire mesh demister in the floss hole offered below oxidizing tower side;
Step 3, flue gas enter denitrating tower from bottom, and have three layers in tower spray, and ground floor slurries are the alkaline absorbent solution in slurry pool, are transported to underlying nozzle spray by circulating pump, and second layer spray is external H
2o
2solution spraying, third layer slurries are the alkaline absorbent solution in slurry pool, and be delivered to upper strata nozzle spray by circulating pump, reach and first absorb the resorbent process of rear oxidation, the flue gas after purification, by smoke stack emission after the demister demist above denitrating tower.
2. the implementation method of the distributed desulfurizing and denitrifying process of a kind of boiler smoke integration according to claim 1, it is characterized in that: be void tower structure in described desulfurizing tower (1), material is warm glass flake in carbon steel lining, two-layer spraying layer is provided with in tower, spraying layer adopts glass reinforced plastic pipe and nozzle, and the gas-liquid contact mode of employing is the mode of reverse spray.
3. according to claim 1 and 2, it is characterized in that: in order to adapt to the change of flue-gas temperature completely, pre-cooled device is set before desulfurizing tower (1) entrance, guarantee that the temperature that flue gas enters absorption tower is less than 120 DEG C.
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|---|---|---|---|
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106178913A (en) * | 2016-08-04 | 2016-12-07 | 中国神华能源股份有限公司 | A kind of flue gas purification system and method |
| WO2017096692A1 (en) * | 2015-12-09 | 2017-06-15 | 深圳广昌达环境科学有限公司 | Fuel gas denitration and desulfurization washing system and denitration and desulfurization method |
| WO2018214990A1 (en) * | 2017-05-25 | 2018-11-29 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of fcc exhaust gas |
| CN109647146A (en) * | 2019-01-23 | 2019-04-19 | 华能国际电力股份有限公司 | System and method for desulfurization and denitrification of industrial boiler flue gas |
| CN109821393A (en) * | 2019-04-08 | 2019-05-31 | 福建省锅炉压力容器检验研究院 | CFB boiler based on wet absorption mixes tail portion flue gas purifying technique after burning sawdust sludge |
| CN112939054A (en) * | 2021-01-19 | 2021-06-11 | 昆明理工大学 | Device and method for preparing copper oxide by using copper nitrate and treating tail gas of copper oxide |
| CN113033961A (en) * | 2021-03-01 | 2021-06-25 | 浙江浙能技术研究院有限公司 | Economic evaluation method of desulfurization synergist |
| CN113521929A (en) * | 2021-08-20 | 2021-10-22 | 骏化生态工程有限公司 | Method for washing particles in tail gas of compound fertilizer |
| CN114432852A (en) * | 2020-10-16 | 2022-05-06 | 中国石油化工股份有限公司 | Processing system of nitre-containing waste gas |
| CN115445417A (en) * | 2022-08-11 | 2022-12-09 | 济南和利时自动化工程有限公司 | Flue gas desulfurization and denitrification integrated system |
| CN115634559A (en) * | 2021-12-31 | 2023-01-24 | 山东庚辰环保新材料有限公司 | Wet desulfurization device, process and application |
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Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2017096692A1 (en) * | 2015-12-09 | 2017-06-15 | 深圳广昌达环境科学有限公司 | Fuel gas denitration and desulfurization washing system and denitration and desulfurization method |
| CN106178913A (en) * | 2016-08-04 | 2016-12-07 | 中国神华能源股份有限公司 | A kind of flue gas purification system and method |
| WO2018214990A1 (en) * | 2017-05-25 | 2018-11-29 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of fcc exhaust gas |
| US10213739B2 (en) | 2017-05-25 | 2019-02-26 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10343110B2 (en) * | 2017-05-25 | 2019-07-09 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10471383B2 (en) | 2017-05-25 | 2019-11-12 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| CN109647146A (en) * | 2019-01-23 | 2019-04-19 | 华能国际电力股份有限公司 | System and method for desulfurization and denitrification of industrial boiler flue gas |
| CN109821393A (en) * | 2019-04-08 | 2019-05-31 | 福建省锅炉压力容器检验研究院 | CFB boiler based on wet absorption mixes tail portion flue gas purifying technique after burning sawdust sludge |
| CN114432852A (en) * | 2020-10-16 | 2022-05-06 | 中国石油化工股份有限公司 | Processing system of nitre-containing waste gas |
| CN112939054A (en) * | 2021-01-19 | 2021-06-11 | 昆明理工大学 | Device and method for preparing copper oxide by using copper nitrate and treating tail gas of copper oxide |
| CN113033961A (en) * | 2021-03-01 | 2021-06-25 | 浙江浙能技术研究院有限公司 | Economic evaluation method of desulfurization synergist |
| CN113033961B (en) * | 2021-03-01 | 2022-07-19 | 浙江浙能技术研究院有限公司 | Economic evaluation method of desulfurization synergist |
| CN113521929A (en) * | 2021-08-20 | 2021-10-22 | 骏化生态工程有限公司 | Method for washing particles in tail gas of compound fertilizer |
| CN115634559A (en) * | 2021-12-31 | 2023-01-24 | 山东庚辰环保新材料有限公司 | Wet desulfurization device, process and application |
| CN115634559B (en) * | 2021-12-31 | 2023-08-04 | 山东庚辰环保新材料有限公司 | Wet desulfurization device, process and application |
| CN115445417A (en) * | 2022-08-11 | 2022-12-09 | 济南和利时自动化工程有限公司 | Flue gas desulfurization and denitrification integrated system |
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