CN104492244A - Waste-gas treating equipment - Google Patents
Waste-gas treating equipment Download PDFInfo
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- CN104492244A CN104492244A CN201410787099.4A CN201410787099A CN104492244A CN 104492244 A CN104492244 A CN 104492244A CN 201410787099 A CN201410787099 A CN 201410787099A CN 104492244 A CN104492244 A CN 104492244A
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- waste gas
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Abstract
The invention relates to waste-gas treating equipment. The waste-gas treating equipment comprises a desulfurization device, a lime supplying device and a wet-type electric precipitator, wherein the desulfurization device comprises a reaction part, a liquid storage part and a spraying part; the lime supplying device is connected with the liquid storage part of the desulfurization device; the wet-type electric precipitator is connected with the spraying part; the lime supplying device supplies lime-gypsum slurry for reaction into the liquid storage part of the desulfurization device; the liquid storage part guides the lime-gypsum slurry into the spraying part by a liquid pump; a spraying nozzle is arranged on the spraying part and sprays the lime-gypsum slurry to the reaction part. Compared with the prior art, the waste-gas treating equipment has the advantages that SO3 in waste gas can be conveniently removed, a new chemical preparation does not need to be introduced, and the blocking of pipelines is reduced.
Description
Technical field
The invention belongs to field of Environment Protection, especially relate to a kind of waste gas treatment equipment.
Background technology
Burnt gas, comprises sulfur oxide, such as SO
2and SO
3, be discharged from an incinerator, wherein fuel package contains at least 0.5wt% sulfur content, and such as heavy fuel or coal fuel are burned.
SO
2at high temperature partially oxidized generation SO
3.SO in flue gas
3air heater can be caused to block or corrode flue, therefore, SO in exhaust
3concentration should be controlled in several below ppm.
Chinese patent CN103007733A discloses the method to the form waste gas of sulfur dioxide process that roasting electrolytic manganese dioxide industry produces, and first compound concentration is the MnO slurry of 50-150g/L, is then placed in plate column or bubbling bed, and what produced by roaster contains SO
2the flue gas of waste gas is introduced in plate column or bubbling bed and is carried out haptoreaction, when the pH of slurry reaches 4.0-5.5, imports in the oxidation bed being provided with online ORP meter, passes into air or oxygen to desulfurization product MnSO
3with Mn (HSO
3)
2be oxidized, when the ORP current potential of online ORP meter display reaches 300mv, show MnSO
3with Mn (HSO
3)
2be oxidized to sulfate completely, stop passing into air or oxygen, obtain MnSO
4solution, directly drains into the reuse of chemical combination workshop by this solution.But for sulfur trioxide, the method cannot do further process.
Summary of the invention
Object of the present invention be exactly in order to overcome above-mentioned prior art exist defect and a kind of SO that can conveniently remove in waste gas is provided
3, do not need the waste gas treatment equipment introducing new chemicals, decrease line clogging.
Object of the present invention can be achieved through the following technical solutions:
A kind of waste gas treatment equipment, and containing SO
3flue connect, this treatment facility comprises desulfurizer, lime feedway and wet electrical dust precipitator,
Described desulfurizer comprises reactive moieties, liquid reservoir divides and blowing portion,
Described lime feedway divides with the liquid reservoir of desulfurizer and is connected,
Described wet electrical dust precipitator is connected with blowing portion,
Described lime feedway provides reaction lime stone-gypsum slurries within the liquid reservoir of desulfurizer divides, lime stone-gypsum slurries are imported to blowing portion by described liquid reservoir lease making liquid pump, described blowing portion is provided with a nozzle, and this nozzle sprays lime stone-gypsum slurries to reactive moieties.
Mg containing 3-5wt% in described lime stone-gypsum slurries.
Lime stone-gypsum slurries are carried out atomization process by described nozzle, form the drop that diameter is 10-100 μm, and after atomization process, the temperature of drop is greater than 130 DEG C.
Preferably, the diameter of drop is 12-18 μm, and after atomization process, the temperature of drop is greater than 140 DEG C.
Described liquid reservoir divides and is also connected with Separation of gypsum device.
Described Separation of gypsum device is connected with sedimentation basin, and sedimentation basin is filtered by membrane separation device, is added to by isolated liquid during liquid reservoir divides.
Described sedimentation basin is also connected with and improves the salt feedway of one or more in NaOH, magnesium hydroxide, sodium sulphate or magnesium sulfate and salt balanced detector.
The supernatant of desulfuration effluent separated in described sedimentation basin is incorporated into through salt spray pump in the two-fluid nozzle in flue, sprays in flue.
Described wet electrical dust precipitator connects washing water tank through washing supply-water pump, sprays into alkaline solution from the upside of wet electrical dust precipitator.
Described alkaline solution is sodium hydroxide solution.
Compared with prior art, the present invention has the following advantages:
1, containing magnesium sulfate based on lime stone-gypsum method desulfurization slurry, being converted into atomization droplet when spraying into the slurries dissolving salt containing this, these the moisture dissolving salt atomization droplet evaporates due to burnt gas.Because the water content of atomization droplet is evaporated, obtain the dry particulate of the particulate atomization of dissolving salt, then, due to SO
3with droplet contact, pollutant is adsorbed by the dry particulate of the salt dissolved and is fixed, and then removes from gas.In brief, because the particulate of the drying of a large amount of little salt dissolved, can by spraying into dissolving salt solution, enough high surface area, it is required for comprising absorption SO in burnt gas
3, promote absorption and pollutant fix.
2, because desulfurization slurry is directed onto the upstream side of desulfurizer, the salt dissolved in the desulfurization slurry sprayed into adsorbs SO in burnt gas
3, the salt of dissolving is collected in desulfurizer, is again used by dissolving circulation.Due to SO
3react with lime, produce gypsum (CaSO
4.2H
2o).Then, the dissolving salt of collection is again injected into and recycles.As mentioned above, because the salt dissolved at desulfurization slurry may not reclaim, the concentration of the salt dissolved in desulfurization slurry can increase.In addition, increase new chemicals and be recovered, operating cost can be reduced significantly.
3, the droplet of simultaneously desulfurization slurry, water content needs evaporation, and the environment that the outlet temperature of blowing portion is equal to or higher than water evaporating temperature is desirable.In addition, the SO that the reaction once together with the salt dissolved occurs
3dew-point temperature or higher be desirable.This is because the temperature below dew point, SO
3gas is converted into SO
3mist, the atomic absorption of the dry salt dissolved is less likely to occur, and therefore reduces removal ability.Therefore, the outlet temperature of blowing portion should be 130 DEG C or more, preferably 140 DEG C or higher.In addition, because be the droplet atomization sprayed into, a two-fluid nozzle is desirable as blowing portion, preferably simultaneously identical with the droplet diameter of a spray aqueous solution by the desulfurization slurry droplet sprayed, water content evaporation floatingization, therefore liquid-drop diameter preferably 10-100 μm are better at 12-18 μm.
4, desulfurizer is based on lime stone-gypsum method, and desulfurizing byproduct is the gypsum of solids content (calcium sulfate) form, and the precipitated pond of this solids content is separated, and solid and liquid is separated.Owing to being separated solids, the liquid recycled has decreased blowing portion blocking.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
In figure, 1-wet electrical dust precipitator, 2-wash supply-water pump, 3-washs water tank, 4-desulfurizer, 5-blowing portion, 6-nozzle, 7-reactive moieties, 8-liquid reservoir divide, 9-two-fluid nozzle, 10-flue, 11-Separation of gypsum device, 12-sedimentation basin, 13-salt balanced detector, 14-salt feedway, 15-salt spray pump, 16-wastewater treatment equipment, 17-lime feedway.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the present invention is described in detail.
Embodiment
A kind of waste gas treatment equipment, its structure as shown in Figure 1, and containing SO
3flue 10 connect, this treatment facility comprises desulfurizer 4, lime feedway 17 and wet electrical dust precipitator 1.Wherein, desulfurizer 4 comprises reactive moieties 7, liquid reservoir divides 8 and blowing portion 5.Lime feedway 17 divides 8 to be connected with the liquid reservoir of desulfurizer 4, and wet electrical dust precipitator 1 is connected with blowing portion 5.
Lime feedway 17 divides in 8 to the liquid reservoir of desulfurizer 4 provides reaction lime stone-gypsum slurries, the Mg containing 3-5wt% in slurries.Liquid reservoir divides 8 through liquid pump, lime stone-gypsum slurries to be imported to blowing portion 5, is provided with a nozzle 6 at blowing portion, and lime stone-gypsum slurries are carried out atomization process by this nozzle 6, forms the drop that diameter is 10-100 μm, and after atomization process, the temperature of drop is greater than 130 DEG C.In order to improve treatment effect, the diameter of drop is 12-18 μm, and after atomization process, the temperature of drop is greater than 140 DEG C, this is because, the droplet of desulfurization slurry, water content needs evaporation, and the environment that the outlet temperature of blowing portion is equal to or higher than water evaporating temperature is desirable.In addition, the SO that the reaction once together with the salt dissolved occurs
3dew-point temperature or higher be desirable.This is because the temperature below dew point, SO
3gas is converted into SO
3mist, the atomic absorption of the dry salt dissolved is less likely to occur, and therefore reduces removal ability.Therefore, the outlet temperature of blowing portion should be 130 DEG C or more, preferably 140 DEG C or higher.In addition, because be the droplet atomization sprayed into, a two-fluid nozzle is desirable as blowing portion, preferably simultaneously identical with the droplet diameter of a spray aqueous solution by the desulfurization slurry droplet sprayed.
Containing magnesium sulfate based on lime stone-gypsum method desulfurization slurry, being converted into atomization droplet when spraying into the slurries dissolving salt containing this, these the moisture dissolving salt atomization droplet evaporates due to burnt gas.Because the water content of atomization droplet is evaporated, obtain the dry particulate of the particulate atomization of dissolving salt, then, due to SO
3with droplet contact, pollutant is adsorbed by the dry particulate of the salt dissolved and is fixed, and then removes from gas.In brief, because the particulate of the drying of a large amount of little salt dissolved, can by spraying into dissolving salt solution, enough high surface area, it is required for comprising absorption SO in burnt gas
3, promote absorption and pollutant fix.
Liquid reservoir divides 8 to be also connected with Separation of gypsum device 11.Separation of gypsum device 11 is connected with sedimentation basin 12, and sedimentation basin 12 is filtered by membrane separation device, isolated liquid is added to liquid reservoir and divides in 8.Sedimentation basin is also connected with and improves the salt feedway 14 of one or more in NaOH, magnesium hydroxide, sodium sulphate or magnesium sulfate and salt balanced detector 13.The supernatant of desulfuration effluent separated in sedimentation basin 12 is incorporated into through salt spray pump 15 in the two-fluid nozzle 9 in flue 10, and some directly enters wastewater treatment equipment 16 and processes.Spray in flue.Wet electrical dust precipitator 1 connects washing water tank 3 through washing supply-water pump 2, sodium hydroxide solution is sprayed into from the upside of wet electrical dust precipitator 1, desulfurizer is based on lime stone-gypsum method, desulfurizing byproduct is the gypsum of solids content (calcium sulfate) form, the precipitated pond of this solids content is separated, and solid and liquid is separated.Owing to being separated solids, the liquid recycled has decreased blowing portion blocking.
Claims (10)
1. a waste gas treatment equipment, and containing SO
3flue connect, it is characterized in that, this treatment facility comprises desulfurizer, lime feedway and wet electrical dust precipitator,
Described desulfurizer comprises reactive moieties, liquid reservoir divides and blowing portion,
Described lime feedway divides with the liquid reservoir of desulfurizer and is connected,
Described wet electrical dust precipitator is connected with blowing portion,
Described lime feedway provides reaction lime stone-gypsum slurries within the liquid reservoir of desulfurizer divides, lime stone-gypsum slurries are imported to blowing portion by described liquid reservoir lease making liquid pump, described blowing portion is provided with a nozzle, and this nozzle sprays lime stone-gypsum slurries to reactive moieties.
2. a kind of waste gas treatment equipment according to claim 1, is characterized in that, the Mg containing 3-5wt% in described lime stone-gypsum slurries.
3. a kind of waste gas treatment equipment according to claim 1, is characterized in that, lime stone-gypsum slurries are carried out atomization process by described nozzle, forms the drop that diameter is 10 μm-100 μm, and after atomization process, the temperature of drop is greater than 130 DEG C.
4. a kind of waste gas treatment equipment according to claim 3, is characterized in that, the preferred 12-18 μm of diameter of described drop, and after atomization process, the temperature of drop is greater than 140 DEG C.
5. a kind of waste gas treatment equipment according to claim 1, is characterized in that, described liquid reservoir divides and is also connected with Separation of gypsum device.
6. a kind of waste gas treatment equipment according to claim 5, is characterized in that, described Separation of gypsum device is connected with sedimentation basin, and sedimentation basin is filtered by membrane separation device, is added to by isolated liquid during liquid reservoir divides.
7. a kind of waste gas treatment equipment according to claim 6, is characterized in that, described sedimentation basin is also connected with and improves the salt feedway of one or more in NaOH, magnesium hydroxide, sodium sulphate or magnesium sulfate and salt balanced detector.
8. a kind of waste gas treatment equipment according to claim 6, is characterized in that, the supernatant of desulfuration effluent separated in described sedimentation basin is incorporated into through salt spray pump in the two-fluid nozzle in flue, sprays in flue.
9. a kind of waste gas treatment equipment according to claim 1, is characterized in that, described wet electrical dust precipitator connects washing water tank through washing supply-water pump, sprays into alkaline solution from the upside of wet electrical dust precipitator.
10. a kind of waste gas treatment equipment according to claim 9, is characterized in that, described alkaline solution is sodium hydroxide solution.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410787099.4A CN104492244A (en) | 2014-12-17 | 2014-12-17 | Waste-gas treating equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410787099.4A CN104492244A (en) | 2014-12-17 | 2014-12-17 | Waste-gas treating equipment |
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| Publication Number | Publication Date |
|---|---|
| CN104492244A true CN104492244A (en) | 2015-04-08 |
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ID=52933748
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|---|---|---|---|
| CN201410787099.4A Pending CN104492244A (en) | 2014-12-17 | 2014-12-17 | Waste-gas treating equipment |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4279873A (en) * | 1978-05-19 | 1981-07-21 | A/S Niro Atomizer | Process for flue gas desulfurization |
| WO1985002453A1 (en) * | 1983-11-25 | 1985-06-06 | Waagner-Biró Aktiengesellschaft | Process for separating acid polluting gas and combustion plant |
| CN1872395A (en) * | 2005-04-26 | 2006-12-06 | 三菱重工业株式会社 | Exhaust gas treatment device and exhaust gas treatment method |
| CN101844819A (en) * | 2010-05-21 | 2010-09-29 | 重庆大学 | Spray evaporation treatment method of wet method flue gas desulfurization wastewater in thermal power station |
| CN203916387U (en) * | 2014-04-25 | 2014-11-05 | 凯天环保科技股份有限公司 | A kind of flue gas device for deep cleaning |
| CN204395762U (en) * | 2014-12-17 | 2015-06-17 | 国网上海市电力公司 | A kind of waste gas treatment equipment |
-
2014
- 2014-12-17 CN CN201410787099.4A patent/CN104492244A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4279873A (en) * | 1978-05-19 | 1981-07-21 | A/S Niro Atomizer | Process for flue gas desulfurization |
| US4279873B1 (en) * | 1978-05-19 | 1996-04-16 | Karsten S Felsvang | Process for flue gas desulferization |
| WO1985002453A1 (en) * | 1983-11-25 | 1985-06-06 | Waagner-Biró Aktiengesellschaft | Process for separating acid polluting gas and combustion plant |
| CN1872395A (en) * | 2005-04-26 | 2006-12-06 | 三菱重工业株式会社 | Exhaust gas treatment device and exhaust gas treatment method |
| CN101844819A (en) * | 2010-05-21 | 2010-09-29 | 重庆大学 | Spray evaporation treatment method of wet method flue gas desulfurization wastewater in thermal power station |
| CN203916387U (en) * | 2014-04-25 | 2014-11-05 | 凯天环保科技股份有限公司 | A kind of flue gas device for deep cleaning |
| CN204395762U (en) * | 2014-12-17 | 2015-06-17 | 国网上海市电力公司 | A kind of waste gas treatment equipment |
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Application publication date: 20150408 |