CN105344214A - Liquid-state catalyst flue gas purification integration system and liquid-state catalyst flue gas purification integration process - Google Patents
Liquid-state catalyst flue gas purification integration system and liquid-state catalyst flue gas purification integration process Download PDFInfo
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- CN105344214A CN105344214A CN201410412544.9A CN201410412544A CN105344214A CN 105344214 A CN105344214 A CN 105344214A CN 201410412544 A CN201410412544 A CN 201410412544A CN 105344214 A CN105344214 A CN 105344214A
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- absorption tower
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- liquid catalyst
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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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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
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Abstract
The present invention relates to a liquid-state catalyst flue gas purification integration system and a liquid-state catalyst flue gas purification integration process. The system comprises an absorption tower, wherein the flue gas inlet of the absorption tower is communicated to a device for supplying oxidized flue gas, the ammonia water inlet of the absorption tower is communicated to an ammonia water supply device, the flue gas outlet of the absorption tower is communicated to a chimney, flue gas in the absorption tower and a liquid-state catalyst and ammonia water are subjected to a countercurrent contact reaction, the mixed salt solution outlet of the absorption tower is sequentially connected to a filter, a separator, and a finished product system, and the liquid-state catalyst outlet of the separator is communicated to the liquid-stage catalyst inlet of the absorption tower. According to the present invention, the system and the process have advantages of high efficiency, low energy consumption, easy operation, low operating cost, no secondary pollution, no waste emission, high-value fertilizer byproduct production and the like; and with the system and the process, sulfur dioxide, nitrogen oxides, mercury, dioxins, fine dust and other pollutants in the flue gas can be removed.
Description
Technical field
The invention belongs to environmental technology field, particularly relate to a kind of employing liquid catalyst gas cleaning integral system and technique thereof, can be used for the process of the pollutants such as the sulfur dioxide in flue gas, nitrogen oxide, mercury, dioxin, fine dust.
Background technology
Sulfur dioxide and nitrogen oxide cause extremely serious harm to our living environment, are wherein produced in combustion by coal, natural gas, heavy oil etc. to a great extent.Sulfur dioxide as the key component of acid rain, to aquatic ecosystem, Agro-ecological System, forest ecosystem, building and material and health all have harm in various degree; Nitrogen oxide, as one of main arch-criminal causing haze weather, directly concerns the process of China's Air Pollution Control to the control of discharged nitrous oxides.At present, the removal methods of sulfur dioxide mainly contains dense flow absorber semidry method, limestone-gypsum method, amine process, SDA semidry method etc., and these methods all come with some shortcomings, as: to the bad adaptability of flue gas, desulfuration efficiency is unstable, and operating cost is high, easily produces secondary pollution etc.The removing process of nitrogen oxide mainly contains SNCR method (SNCR), selective-catalytic-reduction denitrified (SCR), charcoal absorption, electron beam denitration etc., and these methods have shortcomings such as needing the temperature of reaction is high, denitration efficiency is low, easy blocking, operating cost height.
Summary of the invention
The present invention aims to provide a kind of liquid catalyst gas cleaning integral system and technique thereof, for overcoming the many deficiencies existed in prior art, it is high that this device has efficiency, energy consumption is low, simple operation, and operating cost is low, non-secondary pollution and waste discharge, produce the advantages such as the chemical fertilizer byproduct of high value, in addition, the pollutants such as the sulfur dioxide in flue gas, nitrogen oxide, mercury, dioxin, fine dust can also be removed.
The present invention about a kind of technical scheme of liquid catalyst gas cleaning integral system department is, this system comprises absorption tower, at least collecting tank is provided with from the bottom to top in described absorption tower, spray district, except fog-zone, the device that gas approach below spray district, described absorption tower is oxidized flue gas with supply is communicated with, ammoniacal liquor import on the collecting tank of described absorption tower is communicated with ammoniacal liquor feeding mechanism, the air inlet of collecting tank bottom, described absorption tower is communicated with Aeration fan, exhanst gas outlet above described absorption tower demisting district is communicated with chimney, in described absorption tower demisting district, fresh water (FW) inlet channel is installed, between inlet in liquid outlet on the collecting tank of described absorption tower and spray district, described absorption tower, water circle device is installed, the mixture export of described absorption tower sump bottom by excavationg pump successively with filter, separator, finished product system connects, the liquid catalyst outlet of described separator and the liquid catalyst inlet communication on described absorption tower.
Flue gas oxidation in the present invention has multiple method for oxidation, as: ozone oxidation, hydrogen peroxide oxidation, pure oxygen oxidation and air oxidation, wherein, as a kind of preferred embodiment, the device of described supply oxidation flue gas comprises ozone reaction device, the described gas approach of ozone reaction device is communicated with the booster fan of supplied flue gases, the ozone import of described ozone reaction device is communicated with the ozone generator being connected source of the gas, for the oxidation of nitric oxide in flue gas is generated nitrogen dioxide, mercury oxidation generates dimercurion, sulfide-oxidation generates sulfur dioxide, in flue gas, other pollutants such as dioxin have also been obtained fully oxidized.
As a kind of preferred embodiment, described ammoniacal liquor feeding mechanism is the aqua ammonia pump connecting ammonia water tank.
As a kind of preferred embodiment, described finished product system is that the salt liquid storage tank connecting separator is connected with enrichment facility, crystallization granulation device successively, the saline solution be specially in salt liquid storage tank is concentrated into desired concn through enrichment facility rapid evaporation, deliver to crystallization granulation device again and carry out separation finished product crystal, after the finished product crystal obtained is reached requirement by pneumatic conveying drying, pack.
Apply the technique that liquid catalyst gas cleaning integral system of the present invention carries out gas cleaning process, the flue gas comprising the steps: ammoniacal liquor to be delivered in the collecting tank of absorption tower after fully mixing with liquid catalyst and after oxidation carries out counter current contacting reaction, sulfur dioxide in flue gas and nitrogen dioxide are converted into stable ammonium sulfate and ammonium nitrate saline solution, flue gas up to standard after absorbing is discharged from chimney after absorption tower demisting district dewaters, saline solution qualified for concentration is evacuated to after filter removes dust and sediment and delivers to separator, isolated liquid catalyst is recycled in absorption tower and recycles, saline solution is through concentrated, crystallization, granulation, drying obtains finished product chemical fertilizer.
Compared with prior art, liquid catalyst gas cleaning integral system of the present invention has and has superiority as follows: (1) exhaust gas volumn strong adaptability, system run all right, reliable, without line clogging, scale formation;
(2) can recycle ammoniacal liquor, liquid catalyst, realize the treatment of wastes with processes of wastes against one another;
(3) non-secondary pollution thing and waste discharge, there is the ability of synchronized dust removal, desulphurization and denitration and removing heavy-metal mercury and dioxin, and removal efficiency is high, desulfuration efficiency can reach 99%, denitration efficiency can reach 85%, demercuration efficiency can reach 90%, de-dioxin efficiency can reach 50%;
(4) native system can produce the agrochemical ammonium sulfate and ammonium nitrate that meet national standard completely, and operating cost is low, belongs to profitability green technology, and convenient operation is safeguarded, maintenance cost is lower.
Accompanying drawing explanation
Fig. 1 is process chart of the present invention.
1. booster fan, 2. ozone reaction device, 3. ozone generator, 4. source of the gas, 5. ammonia water tank, 6. aqua ammonia pump, 7. Aeration fan, 8. absorption tower, 9. mixed liquor circulating pump, 10. mixed liquor excavationg pump, 11. filters, 12. separators, 13. salt liquid storage tanks, 14. enrichment facilities, 15. crystallization granulation devices.
Detailed description of the invention
A kind of liquid catalyst gas cleaning integral system, comprises booster fan 1, ozone reaction device 2, ozone generator 3, source of the gas 4, ammonia water tank 5, aqua ammonia pump 6, Aeration fan 7, absorption tower 8, mixed liquor circulating pump 9, mixed liquor excavationg pump 10, filter 11, separator 12, salt liquid storage tank 13, enrichment facility 14, crystallization granulation device 15.
The concrete annexation of this system is: the ozone inlet of ozone reaction device 2 connects with the ozone generator 3 being connected source of the gas 4, the gas approach of ozone reaction device 2 is communicated with the booster fan 1 of supplied flue gases, flue gas after oxidation enters absorption tower 8, collecting tank is disposed with from the bottom to top in absorption tower 8, spray district, except fog-zone, described spray district comprises three spraying layers, described fog-zone of removing comprises three layers of demister, absorption tower 8 sprays the outlet of air inlet below district and ozone generator 3, ammoniacal liquor import on the collecting tank of absorption tower 8 is communicated with the aqua ammonia pump 6 being connected ammonia water tank 5, the air inlet of collecting tank bottom, absorption tower 8 is communicated with Aeration fan 7, be communicated with chimney except being provided with exhanst gas outlet above fog-zone on absorption tower 8, in sprayer district, absorption tower 8, fresh water (FW) inlet channel is installed, liquid outlet on the collecting tank of absorption tower 8 is provided with mixed liquor circulating pump 9, for being communicated with the inlet that absorption tower 8 sprays in district, the mixture export of absorption tower 8 sump bottom is communicated with mixed liquor excavationg pump 10, the inlet of filter 11 is communicated with the liquid outlet of mixed liquor circulating pump 9, also dust outlet is provided with bottom described filter 11, the inlet of separator 12 is communicated with the liquid outlet of filter 11, the catalyst outlet of separator 12 is communicated with the catalyst inlet on absorption tower 8, the liquid outlet of separator 12 successively with salt liquid storage tank 13, enrichment facility 14, crystallization granulation device 15 is connected.
Concrete process is: under the effect of ozone strong oxidizing, and oxidation of nitric oxide becomes nitrogen dioxide, mercury oxidation becomes dimercurion, sulfide-oxidation becomes sulfur dioxide, after the material of dioxin have also been obtained and is necessarily oxidized, flue gas after oxidation enters in absorption tower 8 with the speed of about 3.5m/s vertically upward, the Aeration fan 7 of collecting tank bottom, absorption tower 8 makes the mixed liquor of the liquid catalyst in the collecting tank of absorption tower and ammoniacal liquor fully mix, mixed liquor containing liquid catalyst and ammoniacal liquor is evacuated to the spray district on absorption tower 8 by mixed liquor circulating pump 9, spray through shower nozzle the drop that nebulizes to move downward with gravity, the collecting tank on absorption tower 8 is fallen into after vaporific liquid catalyst and the abundant haptoreaction of flue gas upwards, sulfur dioxide in flue gas, nitrogen dioxide will be caught by the liquid catalyst in collecting tank and be oxidized into sulfuric acid and nitric acid, neutralize with ammoniacal liquor, end reaction generates ammonium sulfate and ammonium nitrate, meanwhile, Aeration fan 7 also has an important function, and that is exactly the oxygen content in supplementary mixed liquor, ensures sulfurous acid and nitrous acid complete oxidation, ammoniacal liquor in ammonia water tank 5 is driven in the collecting tank of absorption tower 8 by aqua ammonia pump 6, the acid-base value of mixed liquor is controlled, while desulphurization denitration, liquid catalyst also has extremely strong dissolving adsorption effect to the pollutant such as mercury, dioxin, generates water-fast sediment, remove the neat stress after dust, sulfur dioxide, nitrogen dioxide, mercury, dioxin through absorption tower 8 except fog-zone, remove the moisture in flue gas, be communicated with chimney from the exhaust pass at top, absorption tower 8 and enter air, ammonium sulfate in the collecting tank of absorption tower 8, when ammonium nitrate concn reaches 25% ~ 35%, mixing saline solution excavationg pump 10 will be opened automatically, mixing saline solution enters filter 11, separator 12 is delivered to after dust in filtration removal saline solution and particle, hydrometer method is utilized to be separated, wherein light-phase liquid state catalyst is delivered to absorption tower and is carried out recycling, the unsaturated ammonium sulfate of heavy phase, ammonium nitrate saline solution stores after flowing into salt liquid storage tank 13, mixing saline solution utilizes feed pump to enter enrichment facility 14 by rapid for moisture evaporation and concentration, when material reaches desired concn, open discharging pump and be delivered to crystallization granulation device 15, isolate ammonium sulfate, ammonium nitrate crystals, after crystal is reached moisture requirement by pneumatic conveying drying, obtain finished product sulfuric acid ammonium and ammonium nitrate, pack with packing unit again.
Claims (6)
1. a liquid catalyst gas cleaning integral system, it is characterized in that: comprise absorption tower, at least collecting tank is provided with from the bottom to top in described absorption tower, spray district, except fog-zone, the device that gas approach below spray district, described absorption tower is oxidized flue gas with supply is communicated with, ammoniacal liquor import on the collecting tank of described absorption tower is communicated with ammoniacal liquor feeding mechanism, the air inlet of collecting tank bottom, described absorption tower is communicated with Aeration fan, exhanst gas outlet above described absorption tower demisting district is communicated with chimney, in described absorption tower demisting district, fresh water (FW) inlet channel is installed, between inlet in liquid outlet on the collecting tank of described absorption tower and spray district, described absorption tower, water circle device is installed, the mixture export of described absorption tower sump bottom by excavationg pump successively with filter, separator, finished product system connects, the liquid catalyst outlet of described separator and the liquid catalyst inlet communication on described absorption tower.
2. liquid catalyst gas cleaning integral system as claimed in claim 1, it is characterized in that: the device of described supply oxidation flue gas comprises ozone reaction device, the described gas approach of ozone reaction device is communicated with the booster fan of supplied flue gases, and the ozone import of described ozone reaction device is communicated with the ozone generator being connected source of the gas.
3. liquid catalyst gas cleaning integral system as claimed in claim 1, is characterized in that: described ammoniacal liquor feeding mechanism is the aqua ammonia pump connecting ammonia water tank.
4. liquid catalyst gas cleaning integral system as claimed in claim 1, is characterized in that: described finished product system is that the salt liquid storage tank connecting separator is connected with enrichment facility, crystallization granulation device successively.
5. a liquid catalyst gas cleaning integral process, the flue gas comprising the steps: ammoniacal liquor to be delivered in the collecting tank of absorption tower after fully mixing with liquid catalyst and after oxidation carries out counter current contacting reaction, sulfur dioxide in flue gas and nitrogen dioxide are converted into stable ammonium sulfate and ammonium nitrate saline solution, flue gas up to standard after absorbing is discharged from chimney after absorption tower demisting district dewaters, saline solution qualified for concentration is evacuated to after filter removes dust and sediment and delivers to separator, isolated liquid catalyst is recycled in absorption tower and recycles, saline solution is through concentrated, crystallization, granulation, drying obtains finished product chemical fertilizer.
6. liquid catalyst gas cleaning integral process as claimed in claim 5, is characterized in that: described flue gas oxidation is realized by ozone oxidation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201410412544.9A CN105344214A (en) | 2014-08-21 | 2014-08-21 | Liquid-state catalyst flue gas purification integration system and liquid-state catalyst flue gas purification integration process |
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| CN201410412544.9A CN105344214A (en) | 2014-08-21 | 2014-08-21 | Liquid-state catalyst flue gas purification integration system and liquid-state catalyst flue gas purification integration process |
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| CN105344214A true CN105344214A (en) | 2016-02-24 |
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| CN201410412544.9A Pending CN105344214A (en) | 2014-08-21 | 2014-08-21 | Liquid-state catalyst flue gas purification integration system and liquid-state catalyst flue gas purification integration process |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106115738A (en) * | 2016-06-16 | 2016-11-16 | 济南冶金化工设备有限公司 | Ammonia type flue gas desulfurizing denitration waste liquid enters ammonium sulfate device and produces joint product system |
| CN107159684A (en) * | 2017-06-29 | 2017-09-15 | 浙江富春江环保热电股份有限公司 | Domestic garbage incineration flyash and discarded SCR catalyst coprocessing system and method |
| CN108126490A (en) * | 2017-12-26 | 2018-06-08 | 王静思 | A kind of waste gas cleaning system |
| CN110227328A (en) * | 2019-07-16 | 2019-09-13 | 湖北东方化工有限公司 | A kind of nitric acid flue gas that the rate of recovery is high absorption processing method |
| CN112999844A (en) * | 2021-03-05 | 2021-06-22 | 合肥热电集团有限公司 | Coal-fired power plant flue gas desulfurization and denitrification integrated treatment system and method |
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| CN102500206A (en) * | 2011-08-09 | 2012-06-20 | 中悦浦利莱环保科技有限公司 | System and method for desulfurizing and denitrating smoke based on action of hydrogen peroxide |
| CN102527206A (en) * | 2012-01-16 | 2012-07-04 | 中悦浦利莱环保科技有限公司 | Method and device for treating oxynitride-containing smoke |
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2014
- 2014-08-21 CN CN201410412544.9A patent/CN105344214A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102500206A (en) * | 2011-08-09 | 2012-06-20 | 中悦浦利莱环保科技有限公司 | System and method for desulfurizing and denitrating smoke based on action of hydrogen peroxide |
| CN102527206A (en) * | 2012-01-16 | 2012-07-04 | 中悦浦利莱环保科技有限公司 | Method and device for treating oxynitride-containing smoke |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106115738A (en) * | 2016-06-16 | 2016-11-16 | 济南冶金化工设备有限公司 | Ammonia type flue gas desulfurizing denitration waste liquid enters ammonium sulfate device and produces joint product system |
| CN107159684A (en) * | 2017-06-29 | 2017-09-15 | 浙江富春江环保热电股份有限公司 | Domestic garbage incineration flyash and discarded SCR catalyst coprocessing system and method |
| CN108126490A (en) * | 2017-12-26 | 2018-06-08 | 王静思 | A kind of waste gas cleaning system |
| CN110227328A (en) * | 2019-07-16 | 2019-09-13 | 湖北东方化工有限公司 | A kind of nitric acid flue gas that the rate of recovery is high absorption processing method |
| CN112999844A (en) * | 2021-03-05 | 2021-06-22 | 合肥热电集团有限公司 | Coal-fired power plant flue gas desulfurization and denitrification integrated treatment system and method |
| CN112999844B (en) * | 2021-03-05 | 2022-07-01 | 合肥热电集团有限公司 | Coal-fired power plant flue gas desulfurization and denitrification integrated treatment system and method |
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Application publication date: 20160224 |
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