CN203935765U - A kind of flue gas purification system of integrated desulfurizing denitration - Google Patents
A kind of flue gas purification system of integrated desulfurizing denitration Download PDFInfo
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- CN203935765U CN203935765U CN201420377811.9U CN201420377811U CN203935765U CN 203935765 U CN203935765 U CN 203935765U CN 201420377811 U CN201420377811 U CN 201420377811U CN 203935765 U CN203935765 U CN 203935765U
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- ozone
- flue gas
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 104
- 239000003546 flue gas Substances 0.000 title claims abstract description 104
- 230000003009 desulfurizing effect Effects 0.000 title claims abstract description 21
- 238000000746 purification Methods 0.000 title claims abstract description 21
- 238000010521 absorption reaction Methods 0.000 claims abstract description 124
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 122
- 239000007788 liquid Substances 0.000 claims abstract description 70
- 238000005406 washing Methods 0.000 claims abstract description 57
- 238000005507 spraying Methods 0.000 claims abstract description 46
- 239000007789 gas Substances 0.000 claims abstract description 45
- 239000007921 spray Substances 0.000 claims abstract description 19
- 238000013459 approach Methods 0.000 claims abstract description 17
- 230000008676 import Effects 0.000 claims abstract description 4
- 239000002253 acid Substances 0.000 claims description 15
- 239000012530 fluid Substances 0.000 claims description 9
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 7
- 239000013589 supplement Substances 0.000 claims description 7
- 238000004140 cleaning Methods 0.000 claims description 6
- 230000004907 flux Effects 0.000 claims description 5
- 239000006200 vaporizer Substances 0.000 claims description 5
- 238000012544 monitoring process Methods 0.000 claims description 4
- 238000010276 construction Methods 0.000 claims description 3
- 230000003647 oxidation Effects 0.000 abstract description 58
- 238000007254 oxidation reaction Methods 0.000 abstract description 58
- 238000000034 method Methods 0.000 abstract description 27
- 239000007791 liquid phase Substances 0.000 abstract description 18
- 230000008569 process Effects 0.000 abstract description 13
- 230000000694 effects Effects 0.000 abstract description 10
- 239000012071 phase Substances 0.000 abstract description 6
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 239000003344 environmental pollutant Substances 0.000 description 12
- 239000000203 mixture Substances 0.000 description 12
- 239000002250 absorbent Substances 0.000 description 11
- 230000002745 absorbent Effects 0.000 description 11
- 238000002156 mixing Methods 0.000 description 9
- 231100000719 pollutant Toxicity 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 8
- 239000000779 smoke Substances 0.000 description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 239000013505 freshwater Substances 0.000 description 6
- 238000001179 sorption measurement Methods 0.000 description 6
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000006385 ozonation reaction Methods 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 238000010531 catalytic reduction reaction Methods 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910017604 nitric acid Inorganic materials 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000007115 recruitment Effects 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical group OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- PFRUBEOIWWEFOL-UHFFFAOYSA-N [N].[S] Chemical compound [N].[S] PFRUBEOIWWEFOL-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- -1 on the one hand Chemical compound 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000010186 staining Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000004381 surface treatment Methods 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model provides a kind of flue gas purification system of integrated desulfurizing denitration, comprise: ozone generating-device, washing absorption tower, chimney, wherein, described washing absorption tower comprises the demist layer, spraying layer and the tower reactor that set gradually from top to bottom, outer setting one circulating pump of described tower reactor; Described ozone generating-device is communicated with the gas approach of described washing absorption tower by the first pipeline, and flue gas was mixed with ozone before entering described washing absorption tower; Described ozone generating-device is communicated with described spraying layer by second pipe, and imports ozone in described spray piping, ozone is mixed with absorption liquid after from the ejection of described spraying layer; Described tower reactor is communicated with described spraying layer by described circulating pump; The clean exhanst gas outlet of described washing absorption tower is communicated with described chimney.The utility model flow process is simple, and floor space is little, and cost of investment is low, and the liquid phase oxidation of ozone gas phase, in conjunction with increasing assimilation effect, improves the desulphurization denitration rate of system.
Description
Technical field
The utility model relates to the smoke gas treatment technical fields such as smelting, sintering machine, coal-burning boiler, chemical industry, is specifically related to a kind of flue gas purification system of integrated desulfurizing denitration.
Background technology
The discharge new standard of thermal power plant's atmosphere pollution has significantly tightened up the emission limit of nitrogen oxide, sulfur dioxide and flue dust, formulate the special emission limit of stricter atmosphere pollution for emphasis environment and environmentally sensitive area, and set up the emission limit of mercury and gas fired-boiler.
Along with the increasingly stringent of pollutant control criterion, must remove multiple pollutant simultaneously, if but multi-pollutant is removed respectively, need to introduce many complete equipments, and the problem such as it is huge to face investment, and floor space is many.Multi-pollutant is removed simultaneously and can effectively avoid the problems referred to above, thereby worldwide extensively carried out the research to smoke multi-pollutant control technology.
Various flue gas multiple pollutant new control technologies continue to bring out in recent years, at NOx and SO
2remove, NOx removes than SO
2much more difficult, therefore, mainly from the angle of NO_x removal, study the integrated purified treatment that removes of flue gas multiple pollutant.Based on the angle of NO_x removal, while desulphurization denitration technology can be divided into two classes: a class is catalytic reduction method, mainly utilizes catalyst, reducing agent etc. that NOx is reduced, desulfurization simultaneously; Another kind of is oxidation absorption process, utilizes various strong oxidizers and living radical that water-fast NO oxidation is generated to NO
2thereby, and SO
2absorb in the later stage simultaneously.
(1) catalytic reduction method:
Power plants denitration generally adopts selective catalytic reduction (SCR) technique, and SCR device having relatively high expectations to operating temperature (flue-gas temperature), but under unit underload, exhaust gas temperature reduces, the work cigarette temperature of SCR can not maintain higher temperature, and cold operation easily causes catalyst poisoning to lose efficacy.
(2) oxidation absorption process:
What in oxidation absorption process, commonly use is Ozonation, the problem that can effectively avoid above-mentioned catalytic reduction method to produce, and application prospect is more extensive.It is mainly to remove after utilizing the strong oxidizing property of ozone that the multiple pollutant in flue gas is oxidized to high valence state.The relative additive method energy consumption of Ozonation is low, and in subtractive process, does not need to introduce other materials and cause secondary pollution, and operating temperature is lower simultaneously, is the more promising flue gas desulfurization and denitrification technology of one.Prior art also has more concrete application to Ozonation, and for example patent CN102350190A discloses a kind of flue gas integrated purifying technique and device of while desulphurization denitration.It adds strong oxidizer ozone after air-introduced machine, nitric oxide in flue gas is processed, and by the agent of spray ammonia absorption, the sulfur dioxide in flue gas and nitrogen oxide are removed, utilize strong oxidizer to carry out oxidation processes to sulphite in absorption tower and nitrite simultaneously., there is sulfite oxidation difficulty in the process of this traditional " first and rear oxidation ", oxidation not thoroughly and the problem such as accessory substance complicated component, has limited applying of Ozonation.
To sum up, how solving the technical problem that above-mentioned " first in and rear oxidation " method produces the application of further promoting Ozonation is the problem that those skilled in the art need emphasis to solve.
Utility model content
The purpose of this utility model is to provide a kind of flue gas purification system of integrated desulfurizing denitration, can carry out sufficient oxidation processes to the nitrogen oxide in flue gas and oxysulfide, effectively solves the halfway problem of oxidation.
The technical scheme that the utility model provides is as follows:
A flue gas purification system for integrated desulfurizing denitration, comprising:
Ozone generating-device, washing absorption tower, chimney,
Wherein, described washing absorption tower comprises the demist layer, spraying layer and the tower reactor that set gradually from top to bottom, outer setting one circulating pump of described tower reactor;
Described ozone generating-device is communicated with the gas approach of described washing absorption tower by the first pipeline, and flue gas was mixed with ozone before entering described washing absorption tower; Described ozone generating-device is communicated with described spraying layer by second pipe, and imports ozone in described spray piping, ozone is mixed with absorption liquid after from the ejection of described spraying layer;
Described tower reactor is communicated with described spraying layer by described circulating pump;
The clean exhanst gas outlet of described washing absorption tower is communicated with described chimney.
The flue gas purification system of further preferably, described integrated desulfurizing denitration further comprises:
Air-introduced machine, described the first device for cleaning pipeline is crossed described air-introduced machine and is communicated with the gas approach of described washing absorption tower, and the entrance of described air-introduced machine is communicated with a flue simultaneously, so that the flue gas in the ozone of described the first pipeline and described flue mixed before entering described air-introduced machine.
Further preferably, in described flue, be provided with uniform device;
Further preferably, the gas approach of described washing absorption tower is positioned at the top of described tower reactor;
Further preferably, described spraying layer comprises shower, nozzle, and described shower is multilayer; Described nozzle has hollow cone tangent type structure;
Further preferably, described circulating pump is by the spray flux of spraying layer described in a flow control valve control;
Further preferably, the outside of described tower reactor is also provided with an acid solution excavationg pump, and the interface position of described acid solution excavationg pump and described tower reactor is higher than the interface position of described circulating pump and described tower reactor.
Further preferably, in described tower reactor, be provided with the pH value sensor for monitoring pH in described tower reactor;
Described tower reactor place is communicated with one for supplement the absorption liquid pipeline of absorption liquid to described tower reactor, and an absorption liquid replenishment valve is set in described absorption liquid pipeline.
Further preferably, described demist layer comprises demist filter screen and washer jet, and described washer jet has hollow-core construction.
Further preferably, described ozone generating-device comprises liquid oxygen storage tank, vaporizer and ozone generator;
Further preferably, described second pipe is communicated with described spraying layer by a pair of fluid line, and this two-fluid pipeline is sleeve pipe, comprises inner tube and is placed on the outer tube outside this inner tube, and offering uniform aperture on the tube wall of described inner tube.
The utility model also provides a kind of flue gas purifying method of integrated desulfurizing denitration, and it adopts the flue gas purification system of integrated desulfurizing denitration as the aforementioned, comprises the following steps:
Ozone and flue gas mix entering before the gas approach of described washing absorption tower, and ozone carries out gaseous oxidation to flue gas;
Ozone mixes with the liquid of described circulating-pump outlet, forms ozone-water blend absorbent;
Enter described washing absorption tower with the mixed flue gas of ozone, described ozone-water blend absorbent carries out further liquid phase oxidation through spraying layer spray to flue gas, simultaneously to flue gas desulfurization and denitrification;
Flue gas after desulphurization denitration carries out after demist is dried entering described smoke stack emission through described demister.
Further preferably, after ozone mixes with flue gas, be introduced into described washing absorption tower by air-introduced machine;
Further preferably, ozone mixes with flue gas, and enters described washing absorption tower after uniform in pipeline;
Further preferably, described ozone-water blend absorbent flue gas is oxidized and desulphurization denitration after, reclaim discharging the extraction of carrying out nitrogen and sulphur after tower reactor falling after rise to the solution in described tower reactor.
Further preferably, monitor the pH value of the absorption liquid in described tower reactor, in the time of its pH≤5, the absorption liquid in described tower reactor is discharged;
Further preferably, by described absorption liquid pipeline to described tower reactor supplement absorption liquid, and by described absorption liquid replenishment valve control absorption liquid the liquid level in described tower reactor.
Further preferably, in mixing before described ozone and flue gas are entering the gas approach of described washing absorption tower, the mol ratio of the NO in ozone and the flue gas passing into is 0.8-1.2;
Further preferably, in described ozone mixes with the absorption liquid at described spraying layer place, the SO in ozone and the flue gas passing into
2mol ratio be 0.8-1.2;
Further preferably, the liquid-gas ratio in described washing absorption tower is 7～10L/m
3.
Flue gas purification system and the flue gas purifying method of the integrated desulfurizing denitration providing by the utility model, can bring following at least one beneficial effect:
1. the utility model, by the gas phase of ozone and two kinds of mode combinations of liquid phase oxidation, is strengthened assimilation effect.A part of ozone in ozone generating-device mixes with the flue gas entering before washing absorption tower by the first pipeline, and the NO in flue gas is carried out to sufficient gaseous oxidation; Simultaneously some ozone mixes with the absorption liquid phase in spraying layer in washing absorption tower by second pipe, can be to water-soluble SO in the time spraying
2carry out liquid phase oxidation, oxidation product is SO
4 2-.Ozone can be by SO in liquid-phase oxidation process
2the paramount valence state compound of direct oxidation, without increasing extra oxidation unit, oxidation effectiveness is more abundant, efficiently solves the halfway problem of oxidation of the prior art.
2. oxidation effect.The utility model is introduced the use of the uniform device in air-introduced machine and flue, and the eddy current effect of the uniform and air-introduced machine by flue gas, strengthens the oxidation effectiveness of ozone in gas phase oxidation process.Meanwhile, the second pipe that the utility model is also communicated with spraying layer ozone generating-device adopts the form of sleeve pipe, makes gas-liquid mixed more abundant, strengthens the liquid phase oxidation effect to flue gas.
3. whole system resource consumption of the present utility model is few, operating cost is low, has flow process simple, and floor space is little, and cost of investment is low, denitrification efficiency advantages of higher.
Brief description of the drawings
Below in conjunction with the drawings and specific embodiments, the utility model is described in further detail:
Fig. 1 is the schematic diagram of a kind of embodiment of the flue gas purification system of a kind of integrated desulfurizing denitration of the present utility model.
Drawing reference numeral explanation:
1, flue gas; 2, air-introduced machine; 3, washing absorption tower; 4, circulating pump; 5, spraying layer; 6, nozzle; 7, demist layer; 8, fresh water (FW); 9, purify rear flue gas; 10, chimney; 11, ozone generating-device; 12, gaseous oxidation valve; 13, liquid phase oxidation valve; 14, two-fluid mixing duct; 15, flow control valve; 16, absorption liquid replenishment valve; 17, acid solution excavationg pump.
Detailed description of the invention
In order to be illustrated more clearly in the utility model embodiment or technical scheme of the prior art, to the accompanying drawing of required use in embodiment or description of the Prior Art be briefly described below, apparently, accompanying drawing in the following describes is only embodiment more of the present utility model, for those of ordinary skill in the art, do not paying under the prerequisite of creative work, can also obtain according to these accompanying drawings other accompanying drawing.
In the smoke gas treatment technical fields such as smelting, sintering machine, coal-burning boiler, chemical industry, the pollutant in flue gas is mainly NO and SO
2, in the utility model, utilize ozone gas phase liquid phase oxidation NO and SO
2reaction mechanism as follows:
NO+O
3→NO
2+O
2
NO
2+O
3→NO
3+O
2
SO
2·H
2O(a
q)+O
3→H
2SO
4+O
2
In embodiment mono-of the present utility model, a kind of flue gas purification system of integrated desulfurizing denitration comprises: ozone generating-device, washing absorption tower, chimney, wherein, described washing absorption tower comprises the demist layer, spraying layer and the tower reactor that set gradually from top to bottom, outer setting one circulating pump of described tower reactor; Described ozone generating-device is communicated with the gas approach of described washing absorption tower by the first pipeline, and flue gas was mixed with ozone before entering described washing absorption tower; Described ozone generating-device is communicated with described spraying layer by second pipe, and imports ozone in described spray piping, ozone is mixed with absorption liquid after from the ejection of described spraying layer; Described tower reactor is communicated with described spraying layer by described circulating pump; The clean exhanst gas outlet of described washing absorption tower is communicated with described chimney.The utility model takes full advantage of gaseous oxidation and the liquid phase oxidation characteristic of ozone, on the one hand, ozone mixes with the flue gas before entering washing absorption tower, realizes the abundant oxidation (direct oxidation is high valence state) to nitrogen oxide by the gaseous oxidation of ozone; On the other hand, ozone mixes with the spray-absorption liquid of washing absorption tower inside, can be converted into high valence state to the oxysulfide in flue gas by liquid phase oxidation, and oxidation fully, effectively avoids being oxidized halfway situation.The nitrogen oxide of high valence state and oxysulfide more easily remove and are extracted and recycle.
Ozone generating-device is by the first pipeline (pipeline one, with reference to Fig. 1, the first pipeline place is provided with gaseous oxidation valve 12) be communicated to the flue that the gas approach of washing absorption tower or this gas approach are communicated with, object is to make flue gas to mix with ozone before entering washing absorption tower, nitrogen oxide in flue gas is fully oxidized, is oxidizing to high valence state; Ozone generating-device is by second pipe (pipeline two, with reference to Fig. 1, second pipe place is provided with liquid phase oxidation valve 13) be communicated with the spraying layer in absorption tower, so that ozone is imported in spraying layer and to be mixed with spray liquid, due to ozone pair and the mixed SO of water
2have stronger oxidation, thereby the ozone mixing with spray liquid can be directly by SO
2be oxidizing to high valence state.Spray liquid adsorbs the nitrogen oxide of high valence state and oxysulfide simultaneously, and falls into tower reactor, the nitrogen in solution in tower reactor and sulphur is recycled afterwards again, has completed the abundant oxidation removal of the pollutant to flue gas.Clean flue gas is discharged from the top of washing absorption tower enters chimney, meets the discharge standard of national regulation.The inside of washing absorption tower sets gradually demister, spraying layer and tower reactor from top to bottom, because absorption tower is in running, easily producing particle diameter is " mist " of 10--60 micron, " mist " not only contains moisture, it is also dissolved with sulfuric acid, sulfate, sulfur dioxide etc., also easily causes staining and heavy corrosion of blower fan, heat exchanger and flue, therefore simultaneously, absorption equipment is proposed to the requirement of demist, complete by demister.In tower reactor, there is absorption liquid, and by being located at outside circulating pump, absorption liquid is imported to the spraying layer in tower, flue gas is sprayed to absorption.
Above-described embodiment one is a basic embodiment of the present utility model, also can be optimized it, obtains more preferred embodiment.
Preferably, the utility model also can be introduced air-introduced machine on the basis of embodiment mono-, the first device for cleaning pipeline is crossed air-introduced machine and is communicated with the gas approach of washing absorption tower, and the entrance of air-introduced machine is communicated with a flue simultaneously, so that the flue gas in ozone and the flue of the first pipeline mixed before entering air-introduced machine.Particularly, the entrance of air-introduced machine is communicated with a flue, and extremely described flue of the first pipeline communication, and the outlet of described air-introduced machine is communicated to the gas approach of described washing absorption tower.Can be with reference to Fig. 1, in the flue that flue gas 1 is communicated with at the entrance of air-introduced machine 2, mix with ozone, after the eddy current effect of air-introduced machine, can further strengthen the oxidation effectiveness of ozone to nitrogen oxides in effluent.More preferably, the flue place before air-introduced machine entrance arranges uniform device, can make flue gas be uniformly distributed, and ozone is mixed with flue gas fully, also can strengthen the oxidation effectiveness of ozone to nitrogen oxides in effluent.
Preferably, the gas approach of washing absorption tower is positioned at the top of described tower reactor.
Preferably, the spraying layer in tower reactor comprises shower, nozzle, and shower is multilayer, for example, be 3-5 layer, and spray flux is larger, can improve adsorption efficiency; And nozzle has hollow cone tangent type structure, and simple in structure, atomization is even, easy to use.
Preferably, in basic embodiment for the circulating pump that is communicated with tower reactor and spraying layer by the spray flux of spraying layer described in a flow control valve control, adjusting time easy to use, for example, can regulate according to exhaust gas volumn.
Preferably, the outside of tower reactor is also provided with an acid solution excavationg pump, and the interface position of described acid solution excavationg pump and described tower reactor is higher than the interface position of described circulating pump and described tower reactor.Because the absorption liquid of tower reactor inside circulates between tower reactor and spraying layer, and nitrogen oxide and the oxysulfide of absorption liquid from spraying layer spray and in flue gas carries out adsorption reaction, after operation a period of time, in tower reactor, the pH value of absorption liquid can change, in the utility model, need to monitor this pH value and be greater than 5, otherwise adsorption reaction efficiency will reduce greatly.The pH value sensor of pH in one monitoring tower reactor preferably, is set in tower reactor; After monitoring the pH value of absorption liquid in tower reactor and being less than or equal to 5, by the acid solution excavationg pump being connected with tower reactor, the part solution in tower reactor is discharged.Meanwhile, be communicated with one at tower reactor place for supplement the absorption liquid pipeline of absorption liquid to this tower reactor, after absorption liquid is discharged by acid solution excavationg pump, in tower reactor, supplement new absorption liquid by absorption liquid pipeline; And an absorption liquid replenishment valve is set in absorption liquid pipeline, for controlling the magnitude of recruitment of absorption liquid in tower reactor.
Preferably, the demist layer in tower reactor comprises demist filter screen and washer jet, and described washer jet has hollow-core construction, and the cleaning solution at demist layer place is fresh water (FW) (process water).
In the utility model, ozone generating-device belongs to ozone application technical field, can be discharge type generating means or electrolytic water generator.Discharge type generating means, by electrolysis air or pure oxygen, generates ozone, but wherein the content of foreign gas is higher.The water-soluble formation function water of ozone that electrolytic water generator produces, its ozoniferous purity is higher, is widely used in the fields such as beverage, precise part cleaning, surface treatment.The utility model mainly adopts discharge type generating means.Preferably, ozone generating-device of the present utility model comprises liquid oxygen storage tank, vaporizer and ozone generator, wherein, liquid oxygen storage tank is the low-temperature storage tank for storing liquid oxygen, can replace the repeatedly round transport of gas cylinder, save manpower and cost, be the first-selection of central gas supply; Vaporizer is a kind of industry and civilian energy-saving equipment, and effect is the gas that liquid gas is converted into gaseous state; Ozone generator is for producing ozone gas (O
3) device.Ozone is easy to decompose and cannot stores, and needs scene to produce on-the-spot use (in special situation, can carry out the storage of short time), and the place that can use ozone so every all needs to use ozone generator.In use, the liquid oxygen in liquid oxygen storage tank becomes gaseous oxygen by vaporizer, is produced and is obtained ozone more afterwards by ozone generator.
In use of the present utility model, preferably, described second pipe is communicated with described spraying layer by a pair of fluid line, and this two-fluid pipeline is bushing type pipeline, it comprises inner tube and is placed on the outer tube outside this inner tube, and offers uniform aperture on the tube wall of described inner tube.The inner tube of described bushing type pipeline passes into gas (ozone), outer tube passes into liquid (spray-absorption liquid), on the tube wall of inner tube, have uniform aperture, can make ozone and spray-absorption liquid can realize mixing in sleeve pipe, and be mixed to get comparatively even.Wherein, preferably, the small aperture of offering on inner pipe wall is 3～5cm, and percent opening is 50～60%.With reference to Fig. 1, the liquid phase oxidation valve 13 on second pipe is with check function, prevents liquid backflow.
In a full implementation example of the present utility model, with reference to Fig. 1, the flue gas purification system of integrated desulfurizing denitration of the present utility model comprises air-introduced machine 2, washing absorption tower 3, chimney 10, ozone generating-device 11, washing absorption tower 3 comprises from top to bottom demist layer 7, spraying layer 5 and is positioned at the tower reactor of washing absorption tower 3 bottoms.Flue gas 1 after dedusting enters air-introduced machine 2 from flue, and ozone generating-device is communicated with this flue by the first pipeline (the first pipeline place is provided with gaseous oxidation valve 12), ozone and flue gas are mixed entering before air-introduced machine, and be provided with uniform device in this flue, the mixture of flue gas and ozone is entered in washing absorption tower 3 by the eddy current effect of uniform device and air-introduced machine, and mixing and oxidation effectiveness are all more abundant.Simultaneously the second pipe (second pipe place is provided with liquid phase oxidation valve 13) of ozone generating-device 11 by a telescopic two-fluid mixing duct 14 be communicated with spraying layer 5, the inner tube of two-fluid mixing duct 14 is ozone, it in outer tube, is spray liquid, on inner tubal wall, be evenly equipped with aperture, ozone is fully mixed with spray liquid, obtain ozone-water blend absorbent, and from nozzle 6 ejections.Solution in tower reactor is communicated to spraying layer place by circulating pump 4, is spray liquid, and mixes with ozone, and spray flux is controlled by flow control valve 15.In the time that the pH in tower reactor is less than or equal to 5, by acid solution excavationg pump 17, part solution is discharged, and in tower reactor, supplement new solution by absorption liquid pipeline; And an absorption liquid replenishment valve 16 is set in absorption liquid pipeline, for controlling the magnitude of recruitment of absorption liquid in tower reactor.And the interface position of acid solution excavationg pump 17 and tower reactor is the interface position with tower reactor higher than circulating pump 4.On the top of washing absorption tower 3, demist layer 7 operation water 8 carry out demist to flue gas, and after the purification obtaining, flue gas 9 is discharged from chimney 10.
In a specific embodiment, flue gas condition to be clean is as follows: C (SO
2)=1200mg/m
3, C (NO)=450mg/m
3, 120 DEG C of flue-gas temperatures, enter after dedusting in flue gas purification system of the present utility model, and in the ozone straying quatity of ozone generating-device and flue gas, nitric oxide production mol ratio is 1.0, and tower reactor pH value is controlled at 6.0 left and right, and washing absorption tower liquid-gas ratio is controlled at 8L/m
3, absorbing through the liquid phase oxidation of ozone gas phase, smoke desulfurization efficiency is 95%, denitration efficiency is 80%.
The utility model also provides a kind of flue gas purifying method of integrated desulfurizing denitration, and it has adopted the flue gas purification system of above-mentioned integrated desulfurizing denitration.In an embodiment of flue gas purifying method of the present utility model, comprise the following steps:
Ozone and flue gas mix entering before the gas approach of described washing absorption tower, and ozone carries out gaseous oxidation to flue gas; (step 1)
Ozone mixes with the liquid of described circulating-pump outlet, forms ozone-water blend absorbent; (step 2)
Enter described washing absorption tower with the mixed flue gas of ozone, described ozone-water blend absorbent carries out further liquid phase oxidation through spraying layer spray to flue gas, simultaneously to flue gas desulfurization and denitrification; (step 3)
Flue gas after desulphurization denitration carries out after demist is dried entering described smoke stack emission through described demister.(step 4)
In the embodiment of above-mentioned flue gas purifying method, do not limit the enforcement order of each step, for example step 1 and step 2 just can be carried out simultaneously.This embodiment is the basic embodiment of flue gas purifying method of the present utility model, also can make improvements, and obtains more preferably embodiment.
Preferably, after ozone mixes with flue gas, be introduced into described washing absorption tower by air-introduced machine, can utilize like this eddy current effect of air-introduced machine, strengthen the oxidation effectiveness of ozone to the nitrogen oxide in flue gas.
Preferably, ozone mixes with flue gas, and enters described washing absorption tower after uniform in pipeline.Can by arranging in flue, uniform device be realized ozone and flue gas is mixed uniform, ozone is mixed with flue gas, and then can improve the gaseous oxidation efficiency of ozone.
Preferably, described ozone-water blend absorbent flue gas is oxidized and desulphurization denitration after, falling to the solution in described tower reactor is being discharged to the extraction recovery of carrying out nitrogen and sulphur after tower reactor, so not only can effectively avoid secondary pollution, also can recycle nitrogen sulphur simultaneously, turn waste into wealth.In the time extracting recovery, can make elemental sulfur or nitrogen by technique, or other modes are extracted.
Preferably, in order to ensure the adsorption efficiency of washing absorption tower to pollutant in flue gas, need the pH value that ensures the absorption liquid in tower reactor to be greater than 5, after being less than or equal to 5, adsorption efficiency just has decline by a relatively large margin.Whether one pH value monitor can be set monitors the pH value of absorption liquid in tower reactor and meets the demands.In the time that the pH of absorption liquid in tower reactor value is less than or equal to 5, the absorption liquid in tower reactor is discharged.And can supplement absorption liquid to tower reactor by absorption liquid pipeline, and by the liquid level of an absorption liquid replenishment valve control absorption liquid in tower reactor, control the absorption liquid measure in tower reactor.
Preferably, in the step of mixing before ozone is entering the gas approach of washing absorption tower with flue gas, the mol ratio of NO in ozone and the flue gas passing into is 0.8-1.2, can effectively ensure that like this ozone is more abundant to the nitrogen oxide oxidation in flue gas, and be unlikely to pass into more ozone amount, cause the waste of ozone.In this step, the ozone amount passing into also can be adjusted according to the content of the nitrogen oxide in flue gas, and it is more convenient to use.
Preferably, in the step of mixing with the absorption liquid at spraying layer place at ozone, the SO in ozone and the flue gas passing into
2mol ratio be 0.8-1.2, can effectively ensure that like this ozone is more abundant to the oxidation of oxysulfide, and be unlikely to cause the waste of ozone.In this step, the ozone amount passing into also can be adjusted according to the content of the oxysulfide in flue gas, and it is more convenient to use.
Preferably, the liquid-gas ratio in described washing absorption tower is 7～10L/m
3, can effectively ensure that washing absorption tower operation is safer, and ensure to flue gas internal contamination thing compared with high adsorption rate.
In concrete application of the present utility model, former flue gas after dedusting fully mixes entering before air-introduced machine with from ozone generating-device Yi road ozone gas, NO gas in flue gas is oxidized to high valence state nitrogen oxide, and enter into washing absorption tower, with the ozone-water blend absorbent counter current contacting from spraying layer, NOx and SO
2after the oxidation of absorbent absorption and ozone, be converted into certain density nitric acid and sulfuric acid, and fall after rise in tower reactor.And that flue gas enters the demist of demist layer after desulphurization denitration is dry, finally enter smoke stack emission.Solution in tower reactor is squeezed into spraying layer as absorbent through circulating pump, and mixes with the other road ozone gas from ozone generating-device before entering spraying layer, and the absorption liquid that is dissolved with ozone is to the absorption that circulates of the pollutant in flue gas.In the time that the pH of the solution in tower reactor value is less than 5, part acid solution is discharged through acid solution excavationg pump, and the absorbent in tower reactor is crossed absorption liquid replenishment valve by absorption liquid device for cleaning pipeline and supplemented, and stops supplementing absorption liquid in the time that liquid level reaches requirement.And the acid solution of discharging in tower reactor adopts, and conventional method is concentrated, separation obtains sulfuric acid and nitric acid product.Fresh water (FW) is delivered to demist layer through pressurization and is rinsed, and prevents fouling.
The utility model is by two kinds of mode combinations of ozone gas phase liquid phase oxidation, strengthening assimilation effect, and the liquid phase oxidation of ozone is directly by paramount oxidize sulfur oxides valence state compound, without increasing extra oxidation unit, and the certain density tower reactor acid solution obtaining also can be sold through being further processed into finished product.It is simple that whole system has flow process, and floor space is little, and cost of investment is low, denitrification efficiency advantages of higher, and resource consumption is few, operating cost is low.
It should be noted that all independent assortments as required of above-described embodiment.The above is only preferred embodiment of the present utility model; it should be pointed out that for those skilled in the art, do not departing under the prerequisite of the utility model principle; can also make some improvements and modifications, these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (6)
1. a flue gas purification system for integrated desulfurizing denitration, is characterized in that, comprising:
Ozone generating-device, washing absorption tower, chimney,
Wherein, described washing absorption tower comprises the demist layer, spraying layer and the tower reactor that set gradually from top to bottom, outer setting one circulating pump of described tower reactor;
Described ozone generating-device is communicated with the gas approach of described washing absorption tower by the first pipeline, and flue gas was mixed with ozone before entering described washing absorption tower; Described ozone generating-device is communicated with described spraying layer by second pipe, and imports ozone in described spray piping, ozone is mixed with absorption liquid after from the ejection of described spraying layer;
Described tower reactor is communicated with described spraying layer by described circulating pump;
The clean exhanst gas outlet of described washing absorption tower is communicated with described chimney.
2. the flue gas purification system of integrated desulfurizing denitration according to claim 1, is characterized in that, further comprises:
Air-introduced machine, described the first device for cleaning pipeline is crossed described air-introduced machine and is communicated with the gas approach of described washing absorption tower, and the entrance of described air-introduced machine is communicated with a flue simultaneously, so that the flue gas in the ozone of described the first pipeline and described flue mixed before entering described air-introduced machine.
3. the flue gas purification system of integrated desulfurizing denitration according to claim 2, is characterized in that:
In described flue, be provided with uniform device;
And/or;
The gas approach of described washing absorption tower is positioned at the top of described tower reactor;
And/or;
Described spraying layer comprises shower, nozzle, and described shower is multilayer; Described nozzle has hollow cone tangent type structure;
And/or;
Described circulating pump is by the spray flux of spraying layer described in a flow control valve control;
And/or;
The outside of described tower reactor is also provided with an acid solution excavationg pump, and the interface position of described acid solution excavationg pump and described tower reactor is higher than the interface position of described circulating pump and described tower reactor.
4. the flue gas purification system of integrated desulfurizing denitration according to claim 1, is characterized in that:
In described tower reactor, be provided with the pH value sensor for monitoring pH in described tower reactor;
Described tower reactor place is communicated with one for supplement the absorption liquid pipeline of absorption liquid to described tower reactor, and an absorption liquid replenishment valve is set in described absorption liquid pipeline.
5. the flue gas purification system of integrated desulfurizing denitration according to claim 1, is characterized in that:
Described demist layer comprises demist filter screen and washer jet, and described washer jet has hollow-core construction.
6. according to the flue gas purification system of the integrated desulfurizing denitration described in claim 1-5 any one, it is characterized in that:
Described ozone generating-device comprises liquid oxygen storage tank, vaporizer and ozone generator;
And/or;
Described second pipe is communicated with described spraying layer by a pair of fluid line, and described two-fluid pipeline is bushing type pipeline, and it comprises inner tube and be placed on the outer tube outside this inner tube, and offers uniform aperture on the tube wall of described inner tube.
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| CN201420377811.9U CN203935765U (en) | 2014-07-09 | 2014-07-09 | A kind of flue gas purification system of integrated desulfurizing denitration |
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| CN201420377811.9U CN203935765U (en) | 2014-07-09 | 2014-07-09 | A kind of flue gas purification system of integrated desulfurizing denitration |
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| CN203935765U true CN203935765U (en) | 2014-11-12 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104056538A (en) * | 2014-07-09 | 2014-09-24 | 上海克硫环保科技股份有限公司 | Flue gas purifying system and method with integration of desulfurization and denitrification |
| CN106693586A (en) * | 2017-01-20 | 2017-05-24 | 上海安赐环保科技股份有限公司 | Demisting dedusting system and process for ammonium sulfate dry tail gas |
| CN109260922A (en) * | 2018-11-28 | 2019-01-25 | 广东佳德环保科技有限公司 | A kind of Novel flue gas desulfurization and denitrification integral tower |
| CN113289471A (en) * | 2020-02-24 | 2021-08-24 | 山东师范大学 | Denitration system for flue gas denitration by using ozone and spray tower |
| CN115569497A (en) * | 2022-11-15 | 2023-01-06 | 北京天中方环保科技有限公司 | Desulfurization and denitrification equipment and use method thereof |
-
2014
- 2014-07-09 CN CN201420377811.9U patent/CN203935765U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104056538A (en) * | 2014-07-09 | 2014-09-24 | 上海克硫环保科技股份有限公司 | Flue gas purifying system and method with integration of desulfurization and denitrification |
| CN104056538B (en) * | 2014-07-09 | 2017-01-25 | 上海克硫环保科技股份有限公司 | Flue gas purifying system and method with integration of desulfurization and denitrification |
| CN106693586A (en) * | 2017-01-20 | 2017-05-24 | 上海安赐环保科技股份有限公司 | Demisting dedusting system and process for ammonium sulfate dry tail gas |
| CN109260922A (en) * | 2018-11-28 | 2019-01-25 | 广东佳德环保科技有限公司 | A kind of Novel flue gas desulfurization and denitrification integral tower |
| CN113289471A (en) * | 2020-02-24 | 2021-08-24 | 山东师范大学 | Denitration system for flue gas denitration by using ozone and spray tower |
| CN115569497A (en) * | 2022-11-15 | 2023-01-06 | 北京天中方环保科技有限公司 | Desulfurization and denitrification equipment and use method thereof |
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