CN103386250A - Dry desulphurization method - Google Patents
Dry desulphurization method Download PDFInfo
- Publication number
- CN103386250A CN103386250A CN2013103252743A CN201310325274A CN103386250A CN 103386250 A CN103386250 A CN 103386250A CN 2013103252743 A CN2013103252743 A CN 2013103252743A CN 201310325274 A CN201310325274 A CN 201310325274A CN 103386250 A CN103386250 A CN 103386250A
- Authority
- CN
- China
- Prior art keywords
- desulfurization
- flue gas
- absorbent
- synergistic additives
- dry
- 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.)
- Pending
Links
Images
Abstract
The invention provides a dry desulphurization method comprising the following steps of: introducing raw smoke to a reaction tower, adding a desulphurization absorbent and a synergistic additive into the reaction tower, mixing the desulphurization absorbent, the synergistic additive and the smoke, and reacting to obtain desulphurized purified smoke, wherein the synergistic additive comprises one or more selected from ozone, inorganic peroxide, chlorate, perchlorate, permanganate and perferrate. The synergistic additive adopted in the method is a substance with a strong oxidizing property, the synergistic additive is added into a dry desulphurization smoke treatment system, sulfur dioxide in smoke is converted into sulfur trioxide according to the oxidizing characteristic of the synergistic additive, and the dry desulphurization system has a higher desulphurization effect for sulfur trioxide than sulfur dioxide, thus after the synergistic additive is added in the dry desulphurization process, the sulfur dioxide in the smoke can be remarkably removed, the whole desulphurization efficiency can be increased, and meanwhile, the consumption of the absorbent is reduced.
Description
Technical field
The present invention relates to the desulfur technology field, relate in particular to a kind of method of dry desulfurization.
Background technology
Along with the aggravation of the increasingly strict and environmental problem of environmental regulation,, in order effectively to reduce the discharging of sulfide in flue gas, contain spreading of acid rain, coal-burning power plant adopts different desulfuring and denitrifying apparatus and technique to process to reduce pollution to environment to flue gas one after another.
Flue gas desulfurization technique mainly contains wet desulphurization and the large class of dry desulfurization two at present.The basic principle of wet desulphurization and dry desulfurizing process is all acid-base neutralization, but implementation procedure is different.
Wet desulfurizing process is by the slurries in scrubbing tower, the sulfur dioxide in flue gas to be washed in slurry pool, and then generates stable compound with the lime stone reaction in slurry pool; And dry desulfurizing process generally adopts Circulating Fluidized Bed Process, and it uses the venturi fluidized beds tower as desulfurization reactor take calcium hydroxide as absorbent.Set up the particle layers of high density, fierce turbulence on desulfurizing tower venturi top, by water filling, lower the temperature, make flue-gas temperature be reduced to above 15～20 ℃ of dew point, utilize the relative sliding velocity that produces between flue gas and absorbent granules, realize the purpose of high-efficiency desulfurization.Above-mentioned sulfur method is in to flue gas aspect the removing of sulfur trioxide, and wet desulphurization efficiency is extremely low, and dry desulfurization can almost completely remove the sulfur trioxide in flue gas.But the SO in flue gas
xMajor part is that the form with sulfur dioxide exists, the ratio of sulfur trioxide is lower, and the acidity of sulfur trioxide is strong than sulfur dioxide, faster easier and alkaline absorbent haptoreaction in dry method flue gas desulfur device, although therefore dry desulfurizing process is higher to the absorptivity of the sulfur trioxide in flue gas, but the absorbing and removing efficiency to the sulfur dioxide in flue gas is lower, generally relatively is difficult to reach 90% desulfuration efficiency.
Application number is that the Chinese patent of CN1023327727A discloses a kind of synergist for Wet Limestone-gypsum flue gas desulfurization technique and application thereof.The synergist that this invention is adopted is sodium tetraborate or its hydrate, and it is only applicable to Wet Limestone-desulfurization of gypsum technique, and cardinal principle is to utilize pH value in the shock-absorbing capacity balance wet desulphurization slurries of synergist, thereby the raising wet desulfurizing process is to SO
2Absorption efficiency, but the synergist of foregoing invention and be not suitable as the synergist of dry desulfurization.Therefore, for the present situation of dry desulfurization, the applicant provides a kind of method of dry desulfurization.
Summary of the invention
The technical problem that the present invention solves is to provide a kind of method of dry desulfurization, by method of the present invention, can improve desulfuration efficiency, reduces simultaneously the consumption of absorbent.
In view of this, the invention provides a kind of method of dry desulfurization, comprising:
Desulfurization absorbent is mixed with former flue gas in reaction tower with Synergistic additives, obtain the clean flue gas after desulfurization after reaction; Described Synergistic additives comprises: one or more in ozone, inorganic peroxide, chlorate, perchlorate, permanganate and ferrate.
Preferably, described Synergistic additives is one or more in ozone, potassium hyperchlorate, clorox, sodium chlorite, sodium perchlorate, calcium hypochlorite, hydrogen peroxide and Na2Fe04.
Preferably, described desulfurization absorbent is calcium hydroxide.
Preferably, when described Synergistic additives was gas phase, described Synergistic additives sprayed into flue by the mode of duct injection.
Preferably, when described Synergistic additives was liquid phase, described Synergistic additives sprayed into reaction tower by the mode of spray gun atomization.
Preferably, when described Synergistic additives was solid phase, described Synergistic additives added from the front position of reaction tower.
Preferably, the mol ratio of described Synergistic additives and desulfurization absorbent is (0.01～0.15): 1.
The invention provides a kind of method of dry desulfurization, comprising: desulfurization absorbent is mixed with former flue gas in reaction tower with Synergistic additives, obtain the clean flue gas after desulfurization after reaction; Described Synergistic additives comprises: one or more in ozone, inorganic peroxide, chlorate, perchlorate, permanganate and ferrate.The Synergistic additives that the present invention adopts is the strong oxidizing property material, by Synergistic additives being joined in the dry desulfurization smoke processing system, utilize the oxidation characteristic of Synergistic additives, be sulfur trioxide with the Sulphur Dioxide in flue gas, due to dry method desulfuration system to the removal effect of sulfur trioxide higher than sulfur dioxide, therefore can significantly remove the sulfur dioxide in flue gas in the dry desulfurization process after the interpolation Synergistic additives, improve whole desulfuration efficiency, also reduce the consumption of absorbent simultaneously.
Description of drawings
The dry method flue gas purifier of Fig. 1 prior art desulfurization.
The specific embodiment
In order further to understand the present invention, below in conjunction with embodiment, the preferred embodiment of the invention is described, but should be appreciated that these are described is for further illustrating the features and advantages of the present invention, rather than limiting to the claimed invention.
The invention provides a kind of method of dry desulfurization, comprising: desulfurization absorbent is mixed with former flue gas in reaction tower with Synergistic additives, obtain the clean flue gas after desulfurization after reaction; Described Synergistic additives comprises: one or more in ozone, inorganic peroxide, chlorate, perchlorate, permanganate and ferrate.
According to the present invention, the process of described dry desulfurization gets final product according to process well known to those skilled in the art, the present invention has no particular limits, but need to make flue gas, desulfurization absorbent to mix with Synergistic additives in reaction tower, make Synergistic additives first the part oxidizing sulfur dioxide in flue gas be become sulfur trioxide, then absorbent absorbs the sulfur dioxide in flue gas and sulfur trioxide, thereby removes the oxysulfide in flue gas.
The present invention adopts in the dry desulfurization process Synergistic additives is preferably in ozone, potassium permanganate, clorox, sodium chlorite, sodium perchlorate, calcium hypochlorite, hydrogen peroxide and Na2Fe04 one or more.
The present invention adopts in the dry desulfurization process Synergistic additives is distinguished three kinds of forms is arranged with existence: gas phase, liquid phase and solid phase.The Synergistic additives of described gas phase is take ozone as representative, and the Synergistic additives of described liquid phase is take hydrogen peroxide as representative, and the Synergistic additives of described solid phase is take potassium permanganate, clorox, sodium chlorite or Na2Fe04 as representative.
For the sulfur dioxide in Synergistic additives and flue gas can fully be reacted, the dry desulfurization Synergistic additives of different shape enters the mode of dry method desulfuration system and distinguishes to some extent.As preferred version, gas phase dry desulfurization Synergistic additives adds from the flue before the desulphurization reaction tower, mode by duct injection sprays into flue with Synergistic additives, Synergistic additives evenly mixes with flue gas and with the part sulfur dioxide reaction in flue gas, makes it to be converted into sulfur trioxide, enters subsequently desulfurization reaction tower and carries out desulphurization reaction.
Liquid phase dry desulfurization Synergistic additives front position in desulfurization reaction tower adds, mode by the spray gun atomization sprays into reaction tower with Synergistic additives, make it with flue gas and absorbent can be full and uniform mix and with the part Sulphur Dioxide, be sulfur trioxide, carry out immediately desulphurization reaction.
Solid phase dry desulfurization Synergistic additives adds at desulfurization reaction tower absorbent point of addition, can with add after desulfurization absorbent mixes, also can add separately.After solid phase dry desulfurization Synergistic additives joins in desulfurization reaction tower, its motion state and dry desulfurization absorber class seemingly,, by the abundant haptoreaction with flue gas, can be sulfur trioxide with the part Sulphur Dioxide, then complete the desulphurization reaction with absorbent.
According to the present invention, the mol ratio of described Synergistic additives and desulfurization absorbent is preferably (0.01～0.15): 1, more preferably (0.05～0.10): 1.
Fig. 1 is the dry method flue gas purifier of prior art desulfurization, and wherein 1 is gas approach, and 2 is recirculating fluidized bed reactive absorption tower, and 3 is deduster, 4 is the Matter Transfer air flume, and 5 is the absorbent storehouse, and 6 is the sulfur removal technology water tank, 7 is high-pressure hydraulic pump, and 8 is atomizing lance, and 9 is exhaust pass.Dry method Synergistic additives of the present invention is applicable to the described dry method flue gas purifier of Fig. 1, and also applicable to other dry method flue gas purifier in prior art, the present invention has no particular limits.
The invention provides a kind of method of dry desulfurization, comprising: desulfurization absorbent is mixed with former flue gas in reaction tower with Synergistic additives, obtain the clean flue gas after desulfurization after reaction; Described Synergistic additives comprises: one or more in ozone, inorganic peroxide, chlorate, perchlorate, permanganate and ferrate.The present invention is by joining Synergistic additives in smoke processing system, utilize the oxidation characteristic of Synergistic additives, front end is sulfur trioxide with the part Sulphur Dioxide in dry method desulfuration system desulphurization reaction zone, due to dry method desulfuration system to the removal effect of sulfur trioxide higher than the removal effect to sulfur dioxide, therefore can significantly remove the sulfur dioxide in flue gas in the dry desulfurization process after the interpolation Synergistic additives, improve whole desulfuration efficiency, also reduced the consumption of absorbent simultaneously.
In order further to understand the present invention, below in conjunction with embodiment, the method for dry desulfurization provided by the invention is elaborated, protection scope of the present invention is not limited by the following examples.
Embodiment 1
Certain power generator pool-size is 660MW, and exhaust gas volumn is 4,200,000m
3/ h, former flue gas SO
2Concentration is 3200mg/m
3, adopt dry desulfurization device as shown in Figure 1, adopt the Ca(OH of purity 80%)
2As absorbent, normally moving Ca/S is 1.3, and namely the absorbent use amount is 25.25t/h, select purity be 82% sodium chlorite as desulfurization synergistic additive, the consumption of sodium chlorite is 500kg/h;
The former flue gas that needs to purify enters recirculating fluidized bed reactive absorption tower 2 by gas approach 1, with carry out absorption reaction after recycle stock that the calcium hydroxide that adds from absorbent storehouse 5 and sodium chlorite and Matter Transfer air flume 4 return mixes, complete the process of flue gas desulfurization;
Absorption tower outlet flue gas enters deduster 3, in flue gas unreacted is after the material ash is captured completely, and most of unreacted absorbent calcium hydroxide completely enters the 2 sustainable participations reactions of recirculating fluidized bed absorption tower by Matter Transfer air flume 4 together with absorbent that absorbent storehouse 5 adds.
The results show, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 128mg/m
3, desulfuration efficiency is 96%.
Embodiment 2
Identical with the method for embodiment 1 desulfurization, difference is: the addition of calcium hydroxide is 23.31t/h, and namely adjusting Ca/S is 1.2.The results show, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 256mg/m
3, desulfuration efficiency is 92%, the absorbent consumption has reduced 1.94t/h.
Embodiment 3
Identical with the method for embodiment 1 desulfurization, difference is: the consumption of sodium chlorite is 300kg/h.Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 288mg/m
3, desulfuration efficiency is 91%.
Embodiment 4
Identical with the method for embodiment 1 desulfurization, difference is, the consumption of sodium chlorite is 600kg/h.Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 96mg/m
3, desulfuration efficiency is 97%
Certain power generator pool-size is 660MW, and exhaust gas volumn is 4,200,000m
3/ h, former flue gas SO
2Concentration is 3200mg/m
3, adopt dry desulfurization device as shown in Figure 1, use the Ca(OH of 80% purity)
2As absorbent, normally moving Ca/S is 1.3, and namely the absorbent use amount is 25.25t/h, select purity be 35% hydrogen peroxide as desulfurization synergistic additive, consumption is 1200kg/h.
The former flue gas that needs to purify enters recirculating fluidized bed reactive absorption tower 2 by gas approach 1, after the recycle stock that the absorbent that adds with self-absorption agent storehouse 5 and Matter Transfer air flume 4 return mixes, with be evacuated to through high-pressure hydraulic pump 7 the additive hydrogen peroxide that atomizing lance 8 sprays into from technique water tank 6 and carry out absorption reaction, complete the process of flue gas desulfurization; Absorption tower outlet flue gas enters deduster 3, in flue gas unreacted is after the material ash is captured completely, and most of unreacted absorbent calcium hydroxide completely enters the 2 sustainable participations reactions of recirculating fluidized bed absorption tower by Matter Transfer air flume 4 together with absorbent that absorbent storehouse 5 adds.
Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 160mg/m
3, desulfuration efficiency is 95%.
Embodiment 6
Identical with the method for embodiment 5 desulfurization, difference is: the consumption of calcium hydroxide is 23.31t/h, and namely adjusting Ca/S is 1.2.Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 256mg/m
3, desulfuration efficiency is 92%, the absorbent consumption has reduced 1.94t/h.
Embodiment 7
Identical with the method for embodiment 5 desulfurization, difference is, the consumption of aqueous hydrogen peroxide solution is 900kg/h.Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 256mg/m
3, desulfuration efficiency is 92%.
Embodiment 8
Identical with embodiment 5 sulfur methods, difference is, the consumption of aqueous hydrogen peroxide solution is 1500kg/h.Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 96mg/m
3, desulfuration efficiency is 97%.
Certain power generator pool-size is 660MW, and exhaust gas volumn is 4,200,000m
3/ h, former flue gas SO
2Concentration is 3200mg/m
3, adopt dry desulfurization device as shown in Figure 1, use the Ca(OH of 80% purity)
2As absorbent, normally moving Ca/S is 1.3, and namely the absorbent use amount is 25.25t/h, selects ozone as desulfurization synergistic additive, and consumption is 200kg/h.
The ozone that needs the former flue gas that purifies and ozone generator to produce enters recirculating fluidized bed reactive absorption tower 2 by gas approach 1, carry out absorption reaction after the recycle stock that the absorbent that adds with self-absorption agent storehouse 5 and Matter Transfer air flume 4 return mixes, complete the process of flue gas desulfurization; Absorption tower outlet flue gas enters deduster 3, in flue gas unreacted is after the material ash is captured completely, and most of unreacted absorbent calcium hydroxide completely enters the 2 sustainable participations reactions of recirculating fluidized bed absorption tower by Matter Transfer air flume 4 together with absorbent that absorbent storehouse 5 adds.
Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 224mg/m
3, desulfuration efficiency is 93%.
Embodiment 10
Identical with the method for embodiment 9 desulfurization, difference is: the consumption of calcium hydroxide is 23.31t/h, and namely adjusting Ca/S is 1.2.Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 256mg/m
3, desulfuration efficiency is 92%, the absorbent consumption has reduced 1.94t/h.
Embodiment 11
Identical with the method for embodiment 9 desulfurization, difference is, the consumption of ozone is 100kg/h.Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 288mg/m
3, desulfuration efficiency is 91%.
Embodiment 12
Identical with the method for embodiment 9 desulfurization, difference is, the consumption of ozone is 250kg/h.Experimental result shows, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 160mg/m
3, desulfuration efficiency is 95%.
Comparative Examples 1
Certain power generator pool-size is 660MW, and exhaust gas volumn is 4,200,000m
3/ h, former flue gas SO
2Concentration is 3200mg/m
3, adopt dry desulfurization device as shown in Figure 1, adopt the Ca(OH of purity 80%)
2As absorbent, normally moving Ca/S is 1.3, and namely the absorbent use amount is 25.25t/h;
The former flue gas that need to purify enters recirculating fluidized bed reactive absorption tower 2 by gas approach 1, and carries out absorption reaction after recycle stock that the calcium hydroxide that adds from absorbent storehouse 5 and Matter Transfer air flume 4 return mixes, and completes the process of flue gas desulfurization;
Absorption tower outlet flue gas enters deduster 3, in flue gas unreacted is after the material ash is captured completely, and most of unreacted absorbent calcium hydroxide completely enters the 2 sustainable participations reactions of recirculating fluidized bed absorption tower by Matter Transfer air flume 4 together with absorbent that absorbent storehouse 5 adds.
The results show, after dry desulfurization, the concentration of sulfur dioxide in flue gas is 608mg/m
3, desulfuration efficiency is 81%.
The explanation of above embodiment just is used for helping to understand method of the present invention and core concept thereof.Should be pointed out that for those skilled in the art, under the premise without departing from the principles of the invention, can also carry out some improvement and modification to the present invention, these improvement and modification also fall in the protection domain of the claims in the present invention.
, to the above-mentioned explanation of the disclosed embodiments, make this area professional and technical personnel can realize or use the present invention.Multiple modification to these embodiment will be apparent for those skilled in the art, and General Principle as defined herein can be in the situation that do not break away from the spirit or scope of the present invention, realization in other embodiments.Therefore, the present invention will can not be restricted to these embodiment shown in this article, but will meet the widest scope consistent with principle disclosed herein and features of novelty.
Claims (7)
1. the method for a dry desulfurization, is characterized in that, comprising:
Desulfurization absorbent is mixed with former flue gas in reaction tower with Synergistic additives, obtain the clean flue gas after desulfurization after reaction; Described Synergistic additives comprises: one or more in ozone, inorganic peroxide, chlorate, perchlorate, permanganate and ferrate.
2. method according to claim 1, is characterized in that, described Synergistic additives is one or more in ozone, potassium hyperchlorate, clorox, sodium chlorite, sodium perchlorate, calcium hypochlorite, hydrogen peroxide and Na2Fe04.
3. method according to claim 1, is characterized in that, described desulfurization absorbent is calcium hydroxide.
4. method according to claim 1, is characterized in that, when described Synergistic additives was gas phase, the mode of described Synergistic additives by duct injection sprayed into the flue before desulfurization reaction tower.
5. method according to claim 1, is characterized in that, when described Synergistic additives was liquid phase, described Synergistic additives sprayed into reaction tower by the mode of spray gun atomization.
6. method according to claim 1, is characterized in that, when described Synergistic additives was solid phase, described Synergistic additives added from the front position of reaction tower.
7. method according to claim 1, is characterized in that, the mol ratio of described Synergistic additives and desulfurization absorbent is (0.01～0.15): 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013103252743A CN103386250A (en) | 2013-07-30 | 2013-07-30 | Dry desulphurization method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013103252743A CN103386250A (en) | 2013-07-30 | 2013-07-30 | Dry desulphurization method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103386250A true CN103386250A (en) | 2013-11-13 |
Family
ID=49530779
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013103252743A Pending CN103386250A (en) | 2013-07-30 | 2013-07-30 | Dry desulphurization method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103386250A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950258A (en) * | 2016-06-22 | 2016-09-21 | 王璐 | Nano sulfur-fixing agent |
| CN107824039A (en) * | 2017-12-04 | 2018-03-23 | 中晶环境科技股份有限公司 | Composite oxidant and the method for dry desulfurization denitration |
| CN110201502A (en) * | 2019-06-27 | 2019-09-06 | 合肥丰德科技股份有限公司 | The efficient dry desulfurizing process of cement kiln flue gas |
| CN112892175A (en) * | 2021-02-02 | 2021-06-04 | 武汉钢铁有限公司 | Method for improving desulfurization effect in desulfurization ash co-processing process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1460033A (en) * | 2001-04-04 | 2003-12-03 | 大阪瓦斯株式会社 | Desulfurizer and method of desulfurization |
| CN1539546A (en) * | 2003-11-02 | 2004-10-27 | 华北电力大学 | Method and equipment of desulfurization and denitrogenation for purifying flue gas |
| CN1720091A (en) * | 2002-10-01 | 2006-01-11 | 艾尔波清洁能源有限公司 | Flue gas purification method |
| CN101695627A (en) * | 2009-10-31 | 2010-04-21 | 福建龙净脱硫脱硝工程有限公司 | Dry-method fume gas purification method and device for synchronous desulfurization and denitrification |
| CN102350208A (en) * | 2011-06-30 | 2012-02-15 | 华北电力大学（保定） | Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof |
-
2013
- 2013-07-30 CN CN2013103252743A patent/CN103386250A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1460033A (en) * | 2001-04-04 | 2003-12-03 | 大阪瓦斯株式会社 | Desulfurizer and method of desulfurization |
| CN1720091A (en) * | 2002-10-01 | 2006-01-11 | 艾尔波清洁能源有限公司 | Flue gas purification method |
| CN1539546A (en) * | 2003-11-02 | 2004-10-27 | 华北电力大学 | Method and equipment of desulfurization and denitrogenation for purifying flue gas |
| CN101695627A (en) * | 2009-10-31 | 2010-04-21 | 福建龙净脱硫脱硝工程有限公司 | Dry-method fume gas purification method and device for synchronous desulfurization and denitrification |
| CN102350208A (en) * | 2011-06-30 | 2012-02-15 | 华北电力大学（保定） | Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof |
Non-Patent Citations (3)
| Title |
|---|
| 何晓文: "《水体污染处理新技术及应用》", 31 March 2013, 中国科学技术大学出版社 * |
| 杨延美: "《硫化氢防护培训教材》", 30 April 2011, 中国石化出版社 * |
| 陈震阳: "《现代分析技术在环境与卫生监测中的应用》", 31 August 1995, 中国环境科学出版社 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105950258A (en) * | 2016-06-22 | 2016-09-21 | 王璐 | Nano sulfur-fixing agent |
| CN107824039A (en) * | 2017-12-04 | 2018-03-23 | 中晶环境科技股份有限公司 | Composite oxidant and the method for dry desulfurization denitration |
| CN110201502A (en) * | 2019-06-27 | 2019-09-06 | 合肥丰德科技股份有限公司 | The efficient dry desulfurizing process of cement kiln flue gas |
| CN112892175A (en) * | 2021-02-02 | 2021-06-04 | 武汉钢铁有限公司 | Method for improving desulfurization effect in desulfurization ash co-processing process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2952395C (en) | Process and device for desulfurization-denitration of flue gas | |
| CN103566725B (en) | A kind of circulating fluid bed semi-drying method combined desulfurization and denitration mercury removal device and method | |
| CN103894047B (en) | Flue gas pollutant controls integrated purifying recovery process | |
| CN102350208B (en) | Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof | |
| CN102274681A (en) | Hydrogen-hydroxide-based flue gas synchronous desulfuration and denitration system and method | |
| CN104906937A (en) | Flue gas desulfurization and denitrification device and method of coal fired boiler | |
| CN103877839A (en) | Flue gas pollutant control integrated purification process | |
| CN102921287A (en) | Double-tower double-circulation limestone wet method desulfurization device and method | |
| CN104258701B (en) | Smoke denitration method and device | |
| CN104524935B (en) | Single tower type double-cycle spray composite absorption device and method | |
| CN105233647B (en) | A kind of method of ammonium sulfide solution desulphurization denitration | |
| CN104941410A (en) | Flue gas desulfurization and denitrification integrated method and device based on two-step oxidation process of active molecules O3 at low temperature | |
| CN107281924A (en) | A kind of improved ammonia desulfurizing process and system | |
| CN103386250A (en) | Dry desulphurization method | |
| CN103801177B (en) | A kind of flue gas processing method of calcium magnesium processes simultaneous SO_2 and NO removal demercuration | |
| CN102327735A (en) | Hydrogen peroxide-based flue-gas desulfurizing and denitrifying system and method | |
| CN102824814A (en) | Wet-type redox desulfurizing and recycling method for smoke | |
| CN103100294A (en) | Method for removing oxynitride from flue gas through ozone oxidation method | |
| CN102698583B (en) | Method and device for desulfurizing tail gas of ship engine by electrolytic method by using sea water | |
| CN113769564B (en) | Semi-dry desulfurization ash solidified industrial flue gas carbon dioxide and recycling method thereof | |
| CN102114384B (en) | Flue gas denitration addition agent | |
| CN203090746U (en) | Desulfurization and denitrification integrated device for smoke | |
| CN203108371U (en) | Special device for flue gas dust removal desulfurization and denitrification process | |
| CN113117483A (en) | Integrated method for dry desulfurization and denitrification and cementing material manufacturing | |
| CN103394275B (en) | Process for synchronously removing SO2 and NOX out of flue gas of coal-fired boiler and controlling haze by seawater method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Owner name: FUJIAN LONGKING CO., LTD. Effective date: 20140825 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20140825 Address after: 7 floor A, block 399, Lin Lu, Huli District, Fujian, Xiamen, China, 361009 Applicant after: Fujian Longking Desulphurization & Denitrification Engineering Co., Ltd. Applicant after: Fujian Longking Co., Ltd. Address before: 7 floor A, block 399, Lin Lu, Huli District, Fujian, Xiamen, China, 361009 Applicant before: Fujian Longking Desulphurization & Denitrification Engineering Co., Ltd. |
|
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20131113 |
|
| RJ01 | Rejection of invention patent application after publication |