CN205235727U - Desorption system is united to double tower dual cycle wet process oxidation catalysis - Google Patents
Desorption system is united to double tower dual cycle wet process oxidation catalysis Download PDFInfo
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- CN205235727U CN205235727U CN201520882759.7U CN201520882759U CN205235727U CN 205235727 U CN205235727 U CN 205235727U CN 201520882759 U CN201520882759 U CN 201520882759U CN 205235727 U CN205235727 U CN 205235727U
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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
Abstract
Desorption system is united to double tower dual cycle wet process oxidation catalysis, including the two -stage absorption tower, original flue gas at first gets into the one -level absorption tower, adopts wet scrubbing and catalysis technology, the most SO2 of desorption, the flue gas after the desulfurization gets into the flue gas oxidative system, after material oxidations such as NO, hg, gets into secondary absorption tower, adopts pollutants such as SO3 in wet scrubbing and the catalysis technology desorption flue gas, NOx, hg, and clean flue gas is through the chimney evacuation, fresh organic catalyst gets into through the catalyst make -up system secondary absorption tower forms the desulfurization absorption liquid with water after mixing, through with the pollutant reaction after become half new bright absorption liquid, half new bright absorption liquid passes through absorption liquid circulation system and gets into the one -level absorption tower, accomplish desulfurization, oxidation reaction after, the crystallization bottom the one -level absorption tower of the accessory substance ammonium sulfate that forms and ammonium nitrate gets into the chemical fertilizer system that prepares at last, produces high -quality chemical fertilizer. Adoption the method can realize the integrated desorption of pollutants such as SO2, NOx and hg, can also realize the utilization of pollutant simultaneously to it is efficient to have the pollutant desorption, investment cost low grade advantage.
Description
Technical field
The utility model relates to a kind of smoke processing system, and being specifically related to a kind of is boiler of power plant, industrySO in boiler, metallurgy, waste incineration and chemical industry waste gas2, the pollutant such as NOx and Hg entersThe two circulation wet oxidation catalytic associations of row double tower remove system.
Background technology
Coal-fired flue-gas is the main cause that causes China's atmosphere pollution, coal-fired power station boiler and Industrial BoilerThe large coal consumption equipment of China two. China's coal-fired power station boiler mostly configured SCR, ESP (orBF), the equipment such as FGD is to NOx, dust and SO2Control, obtained good result, butAlso there are the following problems: 1. each technique, substantially only for the discharge of Single Pollution thing, causes power plant rawProduction. art chain growth, investment and operating cost increase; 2. China's pollutant emission standard increasingly stringent,Part key area requires near-zero release, and existing Pollutant Control Technology is difficult to meet emission request; 3.Existing Wet Flue Gas Desulfurization Technique also exists clean flue gas drop to carry to cause that dust exceeding, GGH stop up, " stoneCream rain ", chimney burn into desulfurization product is difficult to the problems such as utilization, some areas lime stone demand is alsoBe difficult to meet.
Industry coal-boiler is the second largest coal consumption equipment that is only second to coal-fired electric generation furnace, simultaneously IState's Industrial Boiler exist quantity large, distribute wide, capacity is little, efficiency is low, Pollutant emission concentration is highFeature is the emphasis of next step environmental improvement. But above feature has determined the pollution of Industrial BoilerThing governance model can not imitate that coal-burning power plant sets up ESP, SCR, FGD to dust, NOx andSO2Administer respectively, expensive investment and operating cost considerably beyond Industrial Boiler bear limitDegree.
Pollutant combined removal is the pass of the current coal-fired flue-gas pollution control technology of solution institute ProblemsKey approach, current many R&D institutions remove technology a large amount of research of having opened a business to integrated, as activityBurnt flue gases purification, ozonation technology etc., but because technology is immature, investment and operating costHigh, there is secondary pollution problems and do not apply.
Summary of the invention
The problem existing in order to solve current flue gases purification, the purpose of this utility model is to provideThe two circulation wet oxidation catalytic associations of a kind of double tower remove system, adopt this system can realize SO2、The integrated of the pollutant such as NOx and Hg removes, and can also realize the recycling of pollutant simultaneously,And the advantages such as it is high to have pollutant removing efficiency, and cost of investment is low.
For reaching above object, the utility model adopts following technical scheme:
The two circulation wet oxidation catalytic associations of double tower remove system, comprise first grade absorption tower 1, described oneLevel absorption tower 1 is communicated with two-level absorption tower 3 by flue gas oxidative system 2, described two-level absorption tower 3Outlet is communicated with chimney 4, the 3 absorption liquids outlets of described two-level absorption tower by the slurries circulatory system 5 andDescribed first grade absorption tower 1 absorption liquid entrance is communicated with, described first grade absorption tower 1 bottom and chemical fertilizer preparation systemSystem 6 is communicated with, and described two-level absorption tower 3 absorbs liquid pool and is communicated with catalyst make-up system 7; Described oneLevel is provided with circulated sprinkling system 11 and forced oxidation system 12 in absorption tower 1 from top to bottom, described inIn two-level absorption tower 3, be provided with from top to bottom demister system 33, circulated sprinkling system 31 and force oxygenChange system 32, two-level absorption tower 3 also comprises the fresh water (FW) system 34 being communicated with demister system 33.
In described catalyst make-up system 7, be organic catalyst, described first grade absorption tower 1 and secondary are inhaledReceiving in tower 3 is absorption liquid, and described absorption liquid is the emulsion that organic catalyst and water are re-dubbed.
Described organic catalyst is oil-soluble sulfoxide type organic matter.
In described flue gas oxidative system 2, oxidant adopts H2O2、O3、Cl2、NaClO2、KMnO4The wherein mixture of one or more materials.
Described catalyst make-up system 7, except organic catalyst described in supply, is also added mass concentration and is20～30% ammoniacal liquor, in order to regulate absorption liquid pH value.
The pH value of described first grade absorption tower 1 and two-level absorption tower 3 adopts subregion control, described one-levelThe pH value on absorption tower 1 is controlled at 4.8～5.5, and the pH value of described two-level absorption tower 3 is controlled at 5.8～6.5.
The two circulation wet oxidation catalytic associations of double tower described above remove the removal methods of system, former cigaretteFirst gas enter described first grade absorption tower 1, SO2Water-soluble rear generation H2SO3, and fast by one-levelAbsorption liquid in absorption tower 1 absorbs, and then promotes SO2Absorption, realize most of SO2Remove,Flue gas after desulfurization enters described flue gas oxidative system 2, by after NO and Hg oxidation, then enters instituteState two-level absorption tower 3, the NOx after oxidation and remaining SO2Water-soluble rear formation HNO2And H2SO3，And absorbed by the absorption liquid in two-level absorption tower 3 fast, extracting heavy metal mercury, realizes pollutant simultaneouslyDeep removal, flue gas is emptying through chimney 4; Fresh organic catalyst is through described catalyst make-up system7 enter described two-level absorption tower 3, form desulfurization absorption liquid, warp and pollutant reaction with water after mixingAfter become half fresh absorption liquid, half fresh absorption liquid in two-level absorption tower 3 follows by described absorption liquidLoop systems 5 enters described first grade absorption tower 1, completes after desulfurization, oxidation reaction accessory substance ammonium sulfateIn described first grade absorption tower 1 bottom crystallization, finally enter described chemical fertilizer preparation system 6 with ammonium nitrate,Produce chemical fertilizer.
Compared to the prior art, tool has the following advantages the utility model:
1, the utility model adopts wet oxidation Catalytic processes that pollutant is combined and removed, efficientRemove SO2, NOx, Hg etc. can also produce chemical fertilizer when pollutant, realizes the resource of pollutantChange and utilize, have without CO simultaneously2The advantages such as release, non-secondary pollution, catalyst can recycle.
2, the utility model adopts two-stage absorption tower, and intermediate arrangement dioxygen oxidation system, greatly reducesOxidant consumption, improves oxidant utilization rate, reduces operating cost.
3, the utility model adopts the control of two-stage pH value of absorption column subregion, improves pollutant removing efficiency,Improved accessory substance quality simultaneously.
4, the utility model institute's adopting process and conventional wet sulfur removal technology are similar, and technology is relatively ripe,Much equipment can be general, and improvement cost is low, is applicable to through engineering approaches application.
Brief description of the drawings
Accompanying drawing is the utility model system and method flow chart.
Detailed description of the invention
Below in conjunction with drawings and the specific embodiments, the utility model is described in further detail.
As shown in drawings, the two circulation wet oxidation catalytic associations of the utility model double tower remove system, bagDraw together first grade absorption tower 1, described first grade absorption tower 1 is by flue gas oxidative system 2 and two-level absorption tower 3Be communicated with, described two-level absorption tower 3 outlets are communicated with chimney 4, and described two-level absorption tower 3 absorption liquids go outMouth is communicated with described first grade absorption tower 1 absorption liquid entrance by the slurries circulatory system 5, and described one-level is inhaledReceive tower 1 bottom and be communicated with chemical fertilizer preparation system 6, described two-level absorption tower 3 absorbs liquid pool and catalystMake-up system 7 is communicated with; In described first grade absorption tower 1, be provided with from top to bottom circulated sprinkling system 11With forced oxidation system 12, in described two-level absorption tower 3, be provided with from top to bottom demister system 33,Circulated sprinkling system 31 and forced oxidation system 32, two-level absorption tower 3 also comprises and demister system 33The fresh water (FW) system 34 being communicated with.
As preferred embodiment of the present utility model, in described catalyst make-up system 7, be organic urgingAgent, is absorption liquid in described first grade absorption tower 1 and two-level absorption tower 3, and described absorption liquid is organicThe emulsion that catalyst and water are re-dubbed.
As preferred embodiment of the present utility model, described organic catalyst is that oil-soluble sulfoxide type hasMachine thing.
As preferred embodiment of the present utility model, in described flue gas oxidative system 2, oxidant adoptsH2O2、O3、Cl2、NaClO2、KMnO4The wherein mixture of one or more materials.
As preferred embodiment of the present utility model, described catalyst make-up system 7 is except described in supplyOutside organic catalyst, also add mass concentration and be 20～30% ammoniacal liquor, in order to regulate absorption liquid pHValue.
As preferred embodiment of the present utility model, described first grade absorption tower 1 and two-level absorption tower 3PH value adopt subregion control, the pH value of described first grade absorption tower 1 is controlled at 4.8～5.5, described inThe pH value of two-level absorption tower 3 is controlled at 5.8～6.5.
The two circulation wet oxidation catalytic associations of double tower described above remove the removal methods of system, former cigaretteFirst gas enter described first grade absorption tower 1, SO2Water-soluble rear generation H2SO3, and fast by one-levelAbsorption liquid in absorption tower 1 absorbs, and then promotes SO2Absorption, realize most of SO2Remove,Flue gas after desulfurization enters described flue gas oxidative system 2, by after NO and Hg oxidation, then enters instituteState two-level absorption tower 3, the NOx after oxidation and remaining SO2Water-soluble rear formation HNO2And H2SO3，And absorbed by the absorption liquid in two-level absorption tower 3 fast, extracting heavy metal mercury, realizes pollutant simultaneouslyDeep removal, flue gas is emptying through chimney 4; Fresh organic catalyst is through described catalyst make-up system7 enter described two-level absorption tower 3, form desulfurization absorption liquid, warp and pollutant reaction with water after mixingAfter become half fresh absorption liquid, half fresh absorption liquid in two-level absorption tower 3 follows by described absorption liquidLoop systems 5 enters described first grade absorption tower 1, completes after desulfurization, oxidation reaction accessory substance ammonium sulfateIn described first grade absorption tower 1 bottom crystallization, finally enter described chemical fertilizer preparation system 6 with ammonium nitrate,Production high-quality chemical fertilizer.
As shown in drawings, the utility model adopts wet oxidation catalytic association to remove system, realizes SO2、The integrated of NOx and Hg removes, and adopts two-stage absorption tower, realizes dirty by the control of pH value subregionDye efficiently removing of thing, by two-stage absorption tower intermediate arrangement dioxygen oxidation system, significantly carry simultaneouslyThe utilization rate of hyperoxia agent, reduces oxidant consumption and operating cost.
Claims (5)
1. the two circulation wet oxidation catalytic associations of double tower remove system, comprise first grade absorption tower (1), it is characterized in that: described first grade absorption tower (1) is communicated with two-level absorption tower (3) by flue gas oxidative system (2), described two-level absorption tower (3) outlet is communicated with chimney (4), the outlet of described two-level absorption tower (3) absorption liquid is communicated with described first grade absorption tower (1) absorption liquid entrance by the slurries circulatory system (5), described first grade absorption tower (1) bottom is communicated with chemical fertilizer preparation system (6), described two-level absorption tower (3) absorbs liquid pool and is communicated with catalyst make-up system (7), in described first grade absorption tower (1), be provided with from top to bottom one-level circulated sprinkling system (11) and one-level forced oxidation system (12), in described two-level absorption tower (3), be provided with from top to bottom demister system (33), secondary circulated sprinkling system (31) and secondary forced oxidation system (32), two-level absorption tower (3) also comprises the fresh water (FW) system (34) being communicated with demister system (33).
2. the two circulation wet oxidation catalytic associations of double tower according to claim 1 remove system, it is characterized in that: in described catalyst make-up system (7), be organic catalyst, in described first grade absorption tower (1) and two-level absorption tower (3), be absorption liquid, described absorption liquid is the emulsion that organic catalyst and water are re-dubbed.
3. the two circulation wet oxidation catalytic associations of double tower according to claim 2 remove system, it is characterized in that: described organic catalyst is oil-soluble sulfoxide type organic matter.
4. the two circulation wet oxidation catalytic associations of double tower according to claim 1 remove system, it is characterized in that: described catalyst make-up system (7) is except supply organic catalyst, also add mass concentration and be 20～30% ammoniacal liquor, in order to regulate absorption liquid pH value.
5. the two circulation wet oxidation catalytic associations of double tower according to claim 1 remove system, it is characterized in that: the pH value of described first grade absorption tower (1) and two-level absorption tower (3) adopts subregion control, the pH value of described first grade absorption tower (1) is controlled at 4.8～5.5, and the pH value of described two-level absorption tower (3) is controlled at 5.8～6.5.
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| CN201520882759.7U CN205235727U (en) | 2015-11-06 | 2015-11-06 | Desorption system is united to double tower dual cycle wet process oxidation catalysis |
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| CN201520882759.7U CN205235727U (en) | 2015-11-06 | 2015-11-06 | Desorption system is united to double tower dual cycle wet process oxidation catalysis |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105268294A (en) * | 2015-11-06 | 2016-01-27 | 西安热工研究院有限公司 | Double-tower double-circulation wet oxidation and catalysis combined removal system and method |
| CN106076107A (en) * | 2016-08-04 | 2016-11-09 | 西安热工研究院有限公司 | Hg in a kind of flue gas2+removing System and method for |
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2015
- 2015-11-06 CN CN201520882759.7U patent/CN205235727U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105268294A (en) * | 2015-11-06 | 2016-01-27 | 西安热工研究院有限公司 | Double-tower double-circulation wet oxidation and catalysis combined removal system and method |
| CN106076107A (en) * | 2016-08-04 | 2016-11-09 | 西安热工研究院有限公司 | Hg in a kind of flue gas2+removing System and method for |
| CN106076107B (en) * | 2016-08-04 | 2018-08-07 | 西安热工研究院有限公司 | Hg in a kind of flue gas2+Removing System and method for |
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