CN1475305A - Catalyst for desulfurizing and denitrating at the same time and its application method - Google Patents
Catalyst for desulfurizing and denitrating at the same time and its application method Download PDFInfo
- Publication number
- CN1475305A CN1475305A CNA031456804A CN03145680A CN1475305A CN 1475305 A CN1475305 A CN 1475305A CN A031456804 A CNA031456804 A CN A031456804A CN 03145680 A CN03145680 A CN 03145680A CN 1475305 A CN1475305 A CN 1475305A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- conversion ratio
- ammonium metavanadate
- flue gas
- activated carbon
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Catalysts (AREA)
Abstract
A desulfurizing-denitrating catalyst contains cellular activated carbon (90-99.9 wt.%) and V2O5. It is applied through putting it on supporter in fixed-bed reactor and reacting on fume at 150-250 deg.C and 500-5000/hr of space speed. Its advantage is high transform rate of 80% for SO2 and 50-100% for NO.
Description
Technical field:
The invention belongs to a kind of catalyst and application process thereof, specifically relate to a kind of cellular activated-carbon catalyst and application process thereof at low temperature while desulphurization denitration
Background technology:
The contained SO of coal-fired flue-gas
2And NO
xDischarging be the main cause that forms acid rain and acid mist, ecological environment and health that the mankind are depended on for existence cause great harm, the hidden danger of therefore effectively eliminating the two is imperative.
Flue gas desulfurization of present industrial employing (FGD) and SCR (SCR) technology mostly are two independently technical process.Wherein, coal-fired flue gas desulfurization (FGD) is to control SO at present
2The approach that discharging is commonly used, mainly contain two kinds of wet method and dry method, wet desulfurizing process comparatively ripe (as lime stone-gypsum method) wherein, but the accessory substance that has that equipment is huge, floor space is wide, water consumption is big, produces easily causes the flue gas after secondary pollution and the desulfurization to need heating again shortcoming such as can discharge, and its range of application is restricted.Dry desulfurization has because of it that technology is simple, water consumption is few and is easy to that sulphur resource and flue gas after desulfurization such as can be discharged voluntarily at advantage and has good development prospect.Take off NO at coal-fired flue-gas
xThe field, SCR (SCR) technology is most widely used, as industrial V/TiO
2Catalyst, but existing catalyst must be operated at more than 350 ℃, to avoid because the SO in the flue gas
2With reducing agent NH
3Reaction generates ammonium sulfate and blocks the duct and cause catalysqt deactivation.At present, also have many SO that take off simultaneously
2And NO
xMethod be among the research and development, as Dalian University of Technology's journal, 1996,36 (1): electron beam irradiation, the impulse electric corona technology of 47-50 report; Bull.Chem.Soc.Jpn., Vol.53, No.11, the active carbon and the Ind.Eng.Chem.Res. of 1980:3356 report, Vol.39, the CuO/Al of 2000:3868-3874 report
2O
3Catalyst etc.Yet the former is not suitable for large-scale application because the big operating cost of power consumption is higher; Active carbon because of its lower activity, only is adapted at than low-speed 1000h again
-1Below operation; CuO/Al
2O
3The catalyst operating temperature is at 300～400 ℃, and far above the flue gas exhaust gas temperature of the most of boiler of China, difficult and existing Industrial Boiler mates.In addition, present existing catalyst mostly is graininess greatly, easily causes the gathering of dust in the flue gas, stops up reactor, has limited its practical application in industry.
Summary of the invention:
The purpose of this invention is to provide a kind of simultaneously catalyst and the application process thereof of desulphurization denitration and anti-flue dust at low temperatures.
The percentage by weight of catalyst of the present invention consists of:
Alveolate activated carbon capable 90-99.9%
Vanadic anhydride 0.1～10%;
Catalyst of the present invention is earlier the Alveolate activated carbon capable carrier to be activated, adopt equi-volume impregnating again, with the Alveolate activated carbon capable carrier of the mixed solution of ammonium metavanadate and oxalic acid dipping through overactivation, drying, in inert atmosphere, calcine then, and oxidation and making in air.
Catalyst application process of the present invention is that catalyst is loaded in the fixed bed reactors, and reaction temperature is controlled at 150～250 ℃, feeds the normal pressure flue gas, and air speed is 500～5000h
-1
The Sulfur capacity of catalyst of the present invention is 35～65mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio reaches 50～100%.
The present invention compared with prior art has following advantage:
1. in same reactor, reach desulphurization denitration simultaneously; And be suitable for 150～250 ℃ of uses down of Industrial Boiler flue gas exhaust gas temperature, can mate with existing Industrial Boiler;
2. compare with granular active carbon, Alveolate activated carbon capable has straight-through macropore structure, the percent opening height, gas by the time pressure that produces fall very for a short time, can before dedusting, use;
3. the cellular activated-carbon catalyst that supports of vanadic anhydride has overcome the low activity of active carbon self, easily produces in batch on a large scale, and cost is lower.
The specific embodiment:
Embodiment 1:
Alveolate activated carbon capable at 800 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 48mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.043g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 2%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 200 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 1900h
-1Experimental result is: the Sulfur capacity of catalyst is 45.2mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 82%.
Embodiment 2:
Alveolate activated carbon capable at 850 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 50mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.043g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 2%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 200 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 1820h
-1Experimental result is: the Sulfur capacity of catalyst is 47.3mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 82%.
Embodiment 3:
Alveolate activated carbon capable at 900 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 49mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.043g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 2%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 200 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 1850h
-1Experimental result is: the Sulfur capacity of catalyst is 46.8mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 79%.
Embodiment 4:
Alveolate activated carbon capable at 850 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 48mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.043g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 2%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 180 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 1900h
-1Experimental result is: the Sulfur capacity of catalyst is 55.3mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 50%.
Embodiment 5:
Alveolate activated carbon capable at 850 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 49mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.043g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 2%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 230 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 1850h
-1Experimental result is: the Sulfur capacity of catalyst is 42.8mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is up to 100%.Embodiment 6:
Alveolate activated carbon capable at 850 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 49mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.021g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 1%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 200 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 1880h
-1Experimental result is: the Sulfur capacity of catalyst is 43.6mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 91%.
Embodiment 7:
Alveolate activated carbon capable at 850 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 48mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.064g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 3%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 200 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 1900h
-1Experimental result is: the Sulfur capacity of catalyst is 51.0mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 89%.
Embodiment 8:
Alveolate activated carbon capable at 850 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 48mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.11g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 5%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 200 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol% O
2, Ar is a balance gas, air speed is 1820h
-1Experimental result is: the Sulfur capacity of catalyst is 60.0mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 81%.
Embodiment 9:
Alveolate activated carbon capable at 850 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 49mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.19g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 9%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 200 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 1850h
-1Experimental result is: the Sulfur capacity of catalyst is 84.0mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 60%.
Embodiment 10:
Alveolate activated carbon capable at 850 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 75mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.043g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 2%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 200 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 1200h
-1Experimental result is: the Sulfur capacity of catalyst is 62.1mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 81%.
Embodiment 11:
Alveolate activated carbon capable at 850 ℃ with steam activation 60 minutes, cut into diameter then and be 19mm, highly be the cylindrical fritter of 22mm, adopt equi-volume process, the mixed solution (wherein the concentration of ammonium metavanadate is 0.043g/ml) of dipping ammonium metavanadate and oxalic acid, in 110 ℃ of dryings, then successively in inert atmosphere in calcining and the air oxidation make catalyst, V wherein
2O
5Loading be 2%.
This catalyst is placed on the bracing frame at fixed bed reactors middle part, be warming up to 200 ℃ of ventilations, its simulated flue gas consists of: 1370ppm SO
2, 390ppm NO, 430ppm NH
3, 3vol%H
2O, 3.9vol%O
2, Ar is a balance gas, air speed is 4000h
-1Experimental result is: the Sulfur capacity of catalyst is 39.3mgSO
2/ 100g catalyst is (at SO
2Conversion ratio reaches at 80% o'clock), the NO conversion ratio of this moment is 60%.
Claims (2)
1. desulphurization denitration catalyst simultaneously is characterized in that the percentage by weight of catalyst consists of:
Alveolate activated carbon capable 90-99.9%
Vanadic anhydride 0.1～10%.
2. a kind of while desulphurization denitration Application of Catalyst method as claimed in claim 1 is characterized in that catalyst is loaded in the fixed bed reactors, and reaction temperature is controlled at 150～250 ℃, feeds the normal pressure flue gas, and air speed is 500～5000h
-1
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03145680 CN1212887C (en) | 2003-07-11 | 2003-07-11 | Catalyst for desulfurizing and denitrating at the same time and its application method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03145680 CN1212887C (en) | 2003-07-11 | 2003-07-11 | Catalyst for desulfurizing and denitrating at the same time and its application method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1475305A true CN1475305A (en) | 2004-02-18 |
| CN1212887C CN1212887C (en) | 2005-08-03 |
Family
ID=34155916
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03145680 Expired - Lifetime CN1212887C (en) | 2003-07-11 | 2003-07-11 | Catalyst for desulfurizing and denitrating at the same time and its application method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1212887C (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101979135A (en) * | 2010-10-21 | 2011-02-23 | 张丽莉 | Catalyst for removing NOx and preparation method thereof |
| CN102631838A (en) * | 2011-02-14 | 2012-08-15 | 中国石油化工股份有限公司 | Method for removing NO (nitric oxide) in flue gas |
| CN103263909A (en) * | 2013-05-16 | 2013-08-28 | 太原理工大学 | Method for preparing catalyst for removing SO2 and NO out of cigarette smoke |
| CN103341366A (en) * | 2013-06-27 | 2013-10-09 | 太原师范学院 | Carbon material low-temperature expansion method and preparation method of low-temperature desulphurization and denitration agent for the same |
| CN101559318B (en) * | 2009-05-25 | 2013-10-30 | 天津城市建设学院 | Thermal carbon composite denitration method for coal-fired boiler |
| CN103464139A (en) * | 2013-09-17 | 2013-12-25 | 北京化工大学 | Preparation method of structured flue gas denitrification catalyst |
| CN103691476A (en) * | 2013-12-19 | 2014-04-02 | 海南中航特玻材料有限公司 | Low-temperature synchronous denitration and desulfurization catalyst and preparation method thereof |
| CN107961784A (en) * | 2017-12-12 | 2018-04-27 | 宁波高新区敦和科技有限公司 | A kind of catalyst for flue gas and desulfurizing and denitrifying and preparation method thereof |
| CN108187656A (en) * | 2017-12-30 | 2018-06-22 | 宁波高新区州致科技有限公司 | It is a kind of for catalyst of flue gas and desulfurizing and denitrifying and preparation method thereof |
| CN108612577A (en) * | 2018-04-13 | 2018-10-02 | 哈尔滨工程大学 | A kind of ship activated carbon method tail gas denitrification apparatus and method |
-
2003
- 2003-07-11 CN CN 03145680 patent/CN1212887C/en not_active Expired - Lifetime
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101559318B (en) * | 2009-05-25 | 2013-10-30 | 天津城市建设学院 | Thermal carbon composite denitration method for coal-fired boiler |
| CN101979135B (en) * | 2010-10-21 | 2012-07-04 | 张丽莉 | Catalyst for removing NOx and preparation method thereof |
| CN101979135A (en) * | 2010-10-21 | 2011-02-23 | 张丽莉 | Catalyst for removing NOx and preparation method thereof |
| CN102631838B (en) * | 2011-02-14 | 2014-10-29 | 中国石油化工股份有限公司 | Method for removing NO (nitric oxide) in flue gas |
| CN102631838A (en) * | 2011-02-14 | 2012-08-15 | 中国石油化工股份有限公司 | Method for removing NO (nitric oxide) in flue gas |
| CN103263909A (en) * | 2013-05-16 | 2013-08-28 | 太原理工大学 | Method for preparing catalyst for removing SO2 and NO out of cigarette smoke |
| CN103341366A (en) * | 2013-06-27 | 2013-10-09 | 太原师范学院 | Carbon material low-temperature expansion method and preparation method of low-temperature desulphurization and denitration agent for the same |
| CN103341366B (en) * | 2013-06-27 | 2015-10-28 | 太原师范学院 | The preparation method of a kind of material with carbon element low temperature expansion method and low-temp desulfurization denitrfying agent thereof |
| CN103464139A (en) * | 2013-09-17 | 2013-12-25 | 北京化工大学 | Preparation method of structured flue gas denitrification catalyst |
| CN103464139B (en) * | 2013-09-17 | 2015-11-18 | 北京化工大学 | A kind of preparation method of structured flue gas denitration catalyst |
| CN103691476A (en) * | 2013-12-19 | 2014-04-02 | 海南中航特玻材料有限公司 | Low-temperature synchronous denitration and desulfurization catalyst and preparation method thereof |
| CN103691476B (en) * | 2013-12-19 | 2016-03-30 | 海南中航特玻材料有限公司 | A kind of low-temperature synchronous denitration desulphurization catalyst and preparation method |
| CN107961784A (en) * | 2017-12-12 | 2018-04-27 | 宁波高新区敦和科技有限公司 | A kind of catalyst for flue gas and desulfurizing and denitrifying and preparation method thereof |
| CN108187656A (en) * | 2017-12-30 | 2018-06-22 | 宁波高新区州致科技有限公司 | It is a kind of for catalyst of flue gas and desulfurizing and denitrifying and preparation method thereof |
| CN108612577A (en) * | 2018-04-13 | 2018-10-02 | 哈尔滨工程大学 | A kind of ship activated carbon method tail gas denitrification apparatus and method |
| CN108612577B (en) * | 2018-04-13 | 2021-12-07 | 哈尔滨工程大学 | Device and method for denitration of tail gas of ship by activated carbon method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1212887C (en) | 2005-08-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104941423B (en) | A kind of regeneration fume from catalytic cracking ammonia process of desulfurization denitration dust collecting method and device | |
| CN101856587B (en) | Fluidized activated carbon combined desulfurization and denitrification process | |
| JPH09103646A (en) | Method and apparatus for treating combustion exhaust gas | |
| CN1792455A (en) | Cellular activated-carbon catalyst used for denitrification of flue-gas, prepn. method and application thereof | |
| CN110090541A (en) | A kind of system and method for activated coke combined desulfurization and denitration | |
| CN110624380A (en) | Synergistic desulfurization and denitrification agent and preparation and application thereof | |
| CN1212887C (en) | Catalyst for desulfurizing and denitrating at the same time and its application method | |
| WO2015158139A1 (en) | Preparation method of denitration catalyst for effectively inhibiting oxidation of sulfur dioxide | |
| CN101108304A (en) | Preparation of wave absorbing catalyst and application of the same in purifying flue gas | |
| CN105879879A (en) | High-sulfur-resistant ultralow-temperature SCR (Selective Catalytic Reduction) denitration catalyst and preparation method thereof | |
| CN111905721B (en) | Catalyst for low-temperature denitration and demercuration of titanium dioxide nano array and preparation method thereof | |
| CN112973785A (en) | Catalyst for synergistically removing VOCs and NOx and preparation method thereof | |
| CN107441932A (en) | Fume desulfurizing agent and its production method and application | |
| CN111744501B (en) | Multifunctional environmental catalytic material for tail gas purification and preparation method and application thereof | |
| CN1443595A (en) | Selective reduction catalyst for nitrogen oxide in smoking gas, its preparation method and application | |
| CN106732547B (en) | Demercuration catalyst for low-temperature oxidation of zero-valent mercury in coal-fired flue gas and preparation method thereof | |
| CN1597094A (en) | Honey comb shaped active carbon base catalyst used for sulfur removal and nitrate removal and its preparation and application | |
| CN110961114A (en) | Desulfurization and denitrification catalyst and preparation method thereof | |
| WO2018214360A1 (en) | Neutral complex cleaning liquid for calcium-poisoned denitration catalyst and regeneration method | |
| CN112221488A (en) | Novel core-shell structure catalyst for synergistic denitration and demercuration and preparation method thereof | |
| CN108355680B (en) | Catalyst for cooperatively controlling multiple pollutants in fixed source flue gas and preparation method thereof | |
| CN108837694B (en) | Method for removing zero-valent mercury and fixing ionic mercury from flue gas | |
| CN114887475A (en) | Tail gas treatment method for lithium battery material production | |
| CN107261829A (en) | Low-temperature plasma flue gas denitration method and device for gas-fired boiler | |
| CN1140319C (en) | Desulfurizing technology and system with regenerable metal oxide as desulfurizing agent |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20050803 |