CN109701375A - Resourcebility desulfurization denitration demercuration integral process - Google Patents
Resourcebility desulfurization denitration demercuration integral process Download PDFInfo
- Publication number
- CN109701375A CN109701375A CN201910105962.6A CN201910105962A CN109701375A CN 109701375 A CN109701375 A CN 109701375A CN 201910105962 A CN201910105962 A CN 201910105962A CN 109701375 A CN109701375 A CN 109701375A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- crystallization
- mercury
- resourcebility
- oxidation
- 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
Landscapes
- Treating Waste Gases (AREA)
Abstract
Resourcebility desulfurization denitration demercuration integral process of the present invention, using the oxidation air oxidation NO for going together in the same direction with flue gas being additionally added at NO2And chlorine element is added and aoxidizes HgXAt Hg+2, NO2With slurries and absorbent CaCO3Reaction generates Ca(NO3)2, using wastewater treatment equipment and crystallization apparatus is distilled by Ca(NO3)2Crystallization is precipitated and obtains the high Ca(NO of commercial value3)2·4H2O.Gas mercury ultimately generates HgCL with the chlorine element and oxygen and slurries being added together2And HgO and crystallize or precipitate respectively with calcium nitrate in crystallization apparatus, by malicious secondary heavy metal ion high concentration.
Description
Illustrate: the application is divisional application of the same name, original bill number: 201510134825.7.
Technical field
The present invention relates to a kind of absorption tower process more particularly to a kind of resourcebility desulfurization denitration demercuration integration absorption towers
Technique, each process detail of the present invention can be applied to practical wet desulphurization denitrating technique, and such as spray absorber is filled out
Expect tower, liquid column tower, bubble tower and double loop etc. and various desulphurization denitration absorbents.
Background technique
Patent of invention wet flue gas desulfurization absorption tower for power plant (201110004529.7) and patent of invention wet process of FGD
Absorption tower (201510113730.7) discloses a kind of naked tower technology of the flue gas desulfurization that technique is leading in the world, and the present invention utilizes the dress
It sets or usually wet desulphurization device and existing gypsum dehydration technique, wastewater treatment equipment, again plus the distillation knot of a set of usual technology
Brilliant device, only oxidation air need to be added before absorption tower or in it can be realized 0 cost denitration.
Existing denitration technology has SNCR method, SCR method, low nitrogen burning method, electronic beam method etc., and denitrfying agent has NH3, urea
Deng, but Construction and operation cost is relatively all quite high, and land occupation is larger, makes the more poverty-stricken embarrassment of crowded power plant, and it is lasting to lose.
Existing wet desulphurization device is to soluble Hg2+Removal efficiency about 80% ~ 95%, but free Hg0It is discharged into atmosphere with flue gas, is accounted for
60% or more, Hg of total mercury0 Can exist in an atmosphere and be up to 2 years as long as.Other relatively effective demercuration methods have liquor kalii iodide
Washing, HgCl2Solution washing, sodium sulfide method, chemical oxidization method, photocatalytic oxidation, ultraviolet irradiation etc., but fail to quotient
Industry operation, main cause are that demercuration technology is immature, and operation cost is high, or even very high, do not have pollutant centralization, with ash
Slag, sewage generate secondary pollution, accelerate the period of flue gas mercury pollution beautiful rivers and mountains nothing but.
At present big and small boiler, flue gas generation device will desulphurization denitration, also to go up demercuration in the future, power plant, steel mill,
Glass furnace, sintering machine, cement kiln, Industrial Boiler etc., also to administer PM2.5, administer heavy metal ion, business burden compared with
Weight.
Summary of the invention
The object of the present invention is to provide a kind of resourcebility desulfurization denitration demercuration integral process, reduce construction, operation, dimension
Maintenance cost is protected, air is purified, improves desulfurization denitration demercuration rate.
To achieve the above object, the present invention provides a kind of resourcebility desulfurization denitration demercuration integral process, comprising:
This technique is to patent of invention wet flue gas desulfurization absorption tower for power plant (201110004529.7) and patent of invention wet flue gas
The naked tower process of a kind of flue gas desulfurization that desulfuration absorbing tower (201510113730.7) is announced has carried out further upgrading: utilizing the dress
Oxidation air the oxidation NO, the NO of generation for going together in the same direction with flue gas in setting2 Generation is reacted with water in sprayed slurry on absorption tower
HNO3 To be absorbed, the HNO3With absorbent CaCO in slurries3Reaction generates the nitrate Ca(NO for being highly soluble in water3)2,
In Ca(NO in slurry pool3)2Using plaster slurry pump export section absorption tower slurries to gypsum rotational flow station before crystallization precipitation, and
Gypsum eddy flow overflow slurries in part are imported into desulfurizing waste water processing device, or utilize existing FGD Wastewater Treatment Process
Tower slurries will be partially absorbed and import desulfurizing waste water processing device, to reduce the Ca(NO of slurry pool of absorption tower slurries3 )2 Concentration,
Primary water is obtained using desulfurizing waste water processing device, the primary water is imported into distillation crystallization apparatus evaporative crystallization and obtains Ca
(NO3 )2 ·4H2O。
Steam or distilled water return desulfurizer that the distillation crystallization apparatus is generated or its technique water tank are de- to control
Sulphur denitrating system water balance, or the steam or distilled water are used as boiler replenishing water or other industrial, civil use products,
The steam thermal energy of the distillation crystallization apparatus output can be used as heat tracing or recycling and reusing.
Going together oxidation air in the same direction with flue gas can be using spraying zone oxygen described in patent of invention 201110004529.7
Change air generator to generate；Or NO being capable of oxidation by air generation NO before the absorption tower2 Flue gas warm area be added oxygen
Change air and the coal addition position can extend the oxidization time of NO as far as possible, after air preheater；The oxidation air can
It aperture and is added using flue gas negative pressure into flue, the flue position that oxidation air is added with blower or directly on flue
Place's flue internal oxidition air is uniformly mixed with flue gas to be not required, and is oxidized to original in flue or in absorption tower completely with NO
Then, the additional amount of the oxidation air is so that NO and NO in former flue gas2The NO generated with slurry reaction is in flue or absorption tower
It is inside oxidized to NO completely2 And the NO2It is fully absorbed in time as principle in absorption tower.
Flue-gas temperature for entering the absorption tower is greater than NO2The flue gas of decomposition temperature is importing oxygen into former flue gas
Smoke heat replacing device should be set or cooling measure is taken to drop flue-gas temperature before the flue position of oxidation air needed for changing NO
To NO2Under decomposition temperature, or utilize absorption tower spray reduction flue-gas temperature.
In NO2The former smoke-gas area of heating power decomposition temperature can not make NO oxidation generate NO when the oxidation air is added2,
But when the flue gas reaches NO2 NO will be oxidized to NO when heating power decomposition temperature cigarette district below2 , so not considering to be added
Oxidation air to generatine set heat efficiency, NO oxygenation efficiency and in flue gas when the side effect of other ions, compound, the denitration
Oxidation air used in technique can be added in any flue-gas temperature area before the absorption tower, and such as combustion zone in furnace, economizer enters
Mouthful, air preheater entrance.
The desulfurizing and denitrifying process absorbent can replace with NH3, urea, Ca (OH)2、NaOH、Mg(OH)2, carbide slag,
Seawater, CaO, MgO, Na2O alkaline matter or it is therein several and meanwhile be used as desulfurization denitrification agent.
The absorbent absorbs the technological principle and lime stone CaCO of NO3 It is identical, the isolation technics of the by-product also phase
It is same or similar, for the technique that desulphurization denitration by-product is soluble easily in water, the by-product can be crystallized simultaneously and be mixed
Hefei material, or using the by-product at different temperatures different solubility and it is crystallized respectively, is separated.
HCL or CL is sprayed into the flue gas warm area that mercury can be oxidized2Or HCL and oxygen air or CL2And oxidation air, such as
Before boiler low-temperature superheater suitable position, reheater suitable position, level-one economizer, oxidation gas mercury and reaction generate HgCL2,
HgCL2Then by described device washing, removing, crystallization；HCL or CL2Additional amount according to Hg constituent content in former flue gas and Hg
Removal efficiency determines that CL constituent content can replace the HCL or CL of a part addition in former flue gas2Amount, or even replace completely；Due to cigarette
Bicycle pump content is considerably less, but needs very big, superfluous oxidation air for the oxidation air excess coefficient for being added completely into mercury oxidation
It can be used to subsequent oxidation NO, the oxidation air additional amount should multiply a coefficient to aoxidize NO aequum and determine.
Or the flue gas warm area that can be oxidized in mercury sprays into oxidation air oxidation mercury element, oxidation state mercury and free state mercury and cigarette
SO in gas2, CL element slightly solubility HgO and solubility HgCL are ultimately generated in absorption tower2And by present apparatus washing absorption.
It or include penetrating HCL or CL in combustion zone in furnace before the flue gas stroke at the flue gas warm area position that mercury can be oxidized2,
Or oxygen air or HCL and oxidation air or CL2And oxidation air, mercury element is by the flue gas warm area that can be oxidized in mercury by oxygen
Change.
Using the different solubilities of different dissolved matters at different temperatures crystallization separation process by nitrate crystal with
Mercury ion and the separation of other ionic crystal objects in slurries, to obtain pure nitrate agricultural fertilizer and by the secondary heavy metal of the poison such as mercury
Ion high concentration.
Each technique of the present invention can be applied to usual spray absorber, packed tower, liquid column tower, bubble tower and double
Circuit wet fuel gas desulfurizing technology.
The present invention has following social benefit: the present invention is by patent of invention wet flue gas desulfurization absorption tower for power plant
(201110004529.7) and the further upgrading of patent of invention wet flue gas desulfurization absorption tower (201510113730.7) is allowed into
For a kind of resourcebility desulfurization denitration demercuration integrated apparatus, the installation cost is extremely low, and denitration by-product is a kind of market value
High agricultural fertilizer, while being of great significance to benign ecological cycles, improvement soil, crystallize mercury ion and other heavy metals from
Sub- crystal can be separated with nitrate crystal, centralized processing.
The present apparatus realizes 0 cost of denitrating flue gas demercuration, high profit operation, profit point in deionized water and agricultural fertilizer,
To improve enterprise's desulfurization denitration demercuration enthusiasm, to reach energy-saving and environmental protection, the comprehensive treatment of by-product resource effect
Fruit, to realize the secondary object high concentration of desulfurization denitration demercuration apparatus integration, minimization of cost, by-product resource, poison
Recycling.
Specific embodiment
The present invention will be described in detail below；
1, denitrating technique:
This technique is to patent of invention wet flue gas desulfurization absorption tower for power plant (201110004529.7) and patent of invention wet flue gas
The naked tower technology of a kind of flue gas desulfurization that desulfuration absorbing tower (201510113730.7) is announced has carried out further upgrading: utilizing the dress
The oxidation air oxidation NO for going together in the same direction with flue gas in setting generates NO2 , the NO in absorption tower2It is reacted with water in sprayed slurry
Generate HNO3 To be absorbed, HNO3With absorbent CaCO in sprayed slurry3Reaction generates the substance C a for being highly soluble in water
(NO3)2, in Ca(NO in slurry pool3)2Crystallization is inhaled before being precipitated using absorption tower slurry pump and gypsum dehydration system export section
It receives tower slurries and gypsum eddy flow overflow slurries in part is imported into desulfurizing waste water processing device.Ca(NO3 )2 Concentration reaches certain journey
It will affect denitrification rate when spending close saturation, or even decompose escape again, its saturation degree can be controlled in 50%- in reality controls
100%, tower slurries can will be also partially absorbed using existing FGD Wastewater Treatment Process imports desulfurizing waste water processing device,
But this process flow efficiency is lower, to reduce the Ca(NO in slurry pool of absorption tower slurries3 )2 Concentration utilizes desulfurization wastewater
Processing unit obtains primary water, and the primary water is imported distillation crystallization apparatus evaporative crystallization and obtains Ca(NO3 )2 ·4H2O, nitre
Sour calcium crystal is the very high agricultural fertilizer of agricultural value, while being of great significance to benign ecological cycles, improvement soil.
The steam or distilled water that above-mentioned distillation crystallization apparatus is generated return to desulfurizer or its technique water tank to control water
Balance can be using the steam or distilled water are as boiler replenishing water or other are industrial, civil use because distilled water is deionized water
Steam, distillation aquatic products, the steam thermal energy which generates can be used as industrial pipeline heat tracing or waste heat recycling is sharp again
With.
According to the above, 201110004529.7 institute of patent of invention can be utilized with flue gas oxidation air in the same direction of going together
The spraying zone oxidation air generating device stated generates, or NO can be oxidized generation NO before the absorption tower2 Flue gas temperature
Area's addition oxidation air and the coal addition position can extend the oxidization time of NO as far as possible, after air preheater.Centrifugation can be used
Directly on flue aperture and oxidation air is added into flue using flue gas negative pressure in blower, the cigarette that oxidation air is added
Flue internal oxidition air is uniformly mixed with flue gas at road position is not required, with NO completely by oxygen in flue or in absorption tower
Turn to principle, the amount of the oxidation air is so that NO and NO in former flue gas2The NO generated with slurry reaction in flue or absorbs
NO is oxidized in tower completely2And the NO2 It is fully absorbed in time as principle in absorption tower.
NO2 Heating power decomposition temperature at 150 DEG C or so, in this temperature hereinafter, NO is easy to be oxidised with air to NO2 。
Described is oxidized completely, is absorbed certainly perfect condition completely, and those of ordinary skill can calculate oxidation air
Dosage theoretical value and excess coefficient, the degree of " complete " depends on oxidation air amount, oxidization time, flue gas temperature in practical operation
Degree, flue gas pressure and NO2Complexity, the solubility of by-product and its slurries saturation to react with water, slurries absorbent
All many conditions, the specific values such as degree should determine in practice, and should weigh economy and discharge standard and obtain optimum value, this
Complete degree is exactly the denitrification rate of device, and theoretically the device denitrification rate is very high, can meet the discharge of the existing and following country
Standard.
Flue-gas temperature for entering apparatus of the present invention desulfurization denitration demercuration integration absorption tower is greater than NO2Decomposition temperature
Flue gas should be arranged smoke heat replacing device or adopt before the flue position of the oxidation air needed for importing oxidation NO into former flue gas
Take cooling measure that flue-gas temperature is made to drop to NO2Under decomposition temperature.Or flue-gas temperature, but denitrification rate are reduced using absorption tower spray
It is slightly lower.
In NO2Heating power decomposition temperature cigarette district can not make NO oxidation generate NO when oxidation air is added2, but work as above-mentioned flue gas
Reach NO2 NO will be oxidized to NO when heating power decomposition temperature cigarette district below2 , so not considering oxidation air to unit heat
Efficiency, NO oxygenation efficiency and in flue gas when the side effect of other ions, compound, oxidation used in denitrating technique of the invention
Air can be added in any flue-gas temperature area before the absorption tower, such as combustion zone in furnace, economizer, air preheater entrance etc..
The technique desulphurization denitration absorbent also could alternatively be NH3, urea, Ca (OH)2、NaOH、Mg(OH)2, carbide slag,
Seawater, CaO, MgO, Na2The alkaline matters such as O or it is therein several and meanwhile be used as desulfurization denitrification agent, these absorbents absorb
The technological principle of NO is identical as lime stone, and the isolation technics of by-product is also same or similar, equal for desulphurization denitration by-product
These by-products can be crystallized simultaneously and obtain mixed fertilizer by technique soluble easily in water, or using these by-products not
They are crystallized respectively, are separated by synthermal lower different solubility.
2, hydrargyrum-removing technology:
Using " denitrating technique " device described in aforementioned 1, HCL or CL is sprayed into the flue gas warm area that mercury can be oxidized2Gas, or
CL2And oxidation air or HCL and oxygen air, as boiler low-temperature superheater suitable position, reheater suitable position, level-one save
Before coal device, aoxidizes gas mercury and monovalence mercury and reaction generates HgCL2, HgCL2Then by present apparatus washing, removing, crystallization；HCL
Or CL2Additional amount according in former flue gas the removal efficiency of Hg content and Hg determine, to have certain excess coefficient, former flue gas certainly
The HCL or CL that middle CL constituent content can replace a part to be added2Amount, or even replace completely；Since flue gas mercury content is considerably less, but
Oxidation air excess coefficient to be added completely into mercury oxidation need to be very big, and superfluous oxidation air can be used to subsequent oxidation NO,
Oxidation air additional amount should be multiplied by a safety coefficient to aoxidize NO aequum and determine.
Gas mercury is in 800 ~ 850 K(527 ~ 577 DEG C) Shi Fasheng oxidation reaction, mercury compound be higher than 800 DEG C when decompose,
CL element is easy to react with mercury.
The flue gas warm area that can also can be oxidized in mercury only sprays into oxidation air oxidation mercury element, oxidation state mercury and free state
SO in mercury and flue gas2, CL element slightly solubility HgO and solubility HgCL are ultimately generated in absorption tower2And it is washed and inhales by the present apparatus
It receives: in spraying zone, SO2SO is absorbed as by spray liquid first3 2-, SO3 2-It is oxidized to SO at once4 2-, then aoxidized with alkali metal
Object HgO reaction generates slightly solubility HgSO4(being finally hydrolyzed to subsulfate, HgO precipitating), is then washed and enters slurry pool.
Above-mentioned demercuration oxidant HCL or CL2Or oxygen air or HCL and oxidation air or CL2With oxidation air
Can include before the flue gas stroke at the flue gas warm area that mercury element can be oxidized in furnace combustion zone spray into, mercury element will be
The flue gas warm area that flue gas stroke downstream mercury can be oxidized is oxidized；
2% or so of total mercury is only usually accounted for by the mercury that lime-ash adsorbs, and based on free mercury, after demercuration oxidant is added, trip
It there's almost no from mercury, the presence of CL element has inhibiting effect to particulate matter Adsorption of Mercury, therefore will have more mercury to be absorbed tower
Absorb crystallization, centralization processing, thus by mercury and the secondary ion high concentration of other heavy metals poison, collection, harmless treatment or money
Source.
Using the different solubilities of different dissolved matters at different temperatures crystallization separation process by nitrate crystal with
Mercury ion and the separation of other ionic crystal objects in slurries, to obtain pure nitrate agricultural fertilizer；Due to adding for crystallization processes
Enter, so that the heavy metal ion of toxic side effect crystallizes precipitation together in flue gas, pollutant is focused on or resource
Change.
Since the device is stripped of nitrate, chloride ion, mercury ion and other ions in time, this is reduced in absorption tower
The concentration of a little toxic byproducts, further improves desulfurization degree, reduces corrosion of equipment degree.It can be incited somebody to action by distillation crystallization processes
Nitrate crystallization and mercury ion, villaumite Crystallization Separation.
Present apparatus SO2、NOXWith HgXIt is removed absorption in absorption tower spraying zone simultaneously, and the not phase due to difference of absorbent
It mutually influences, because the naked tower of concurrent-countercurrent has along inverse two flue gas strokes, 1 times more than usual absorption tower soak time, so having enough
Time and space receive these absorbing reactions, for these absorbing reactions, as long as having enough oxidants, absorbent, liquid-gas ratio
L/G and by-product concentration appropriate, these absorption processes, which can be considered as, respectively to be carried out in respective individual absorption tower, mutually
It does not interfere.
Each technique of the present invention can be applied to other wet desulphurization devices to denitration demercuration function
Can, such as spray absorber, packed tower, liquid column tower, bubble tower and double loop wet flue gas desulfurizer.
3, social benefit:
In conclusion the present invention has following social benefit: the present invention is by patent of invention wet flue gas desulfurization absorption tower for power plant
(201110004529.7) and the further upgrading of patent of invention wet flue gas desulfurization absorption tower (201510113730.7) is allowed into
For a kind of resourcebility desulfurization denitration demercuration integrated apparatus, the installation cost is extremely low, and denitration by-product is a kind of market value
High agricultural fertilizer, while being of great significance to benign ecological cycles, improvement soil, crystallize mercury ion and other heavy metals from
Sub- crystal can be separated with nitrate crystal, centralized processing.
The present apparatus realizes 0 cost of denitrating flue gas demercuration, high profit operation, profit point in deionized water and agricultural fertilizer,
To improve enterprise's desulfurization denitration demercuration enthusiasm, to reach energy-saving and environmental protection, the comprehensive treatment of by-product resource effect
Fruit, to realize the secondary object high concentration of desulfurization denitration demercuration apparatus integration, minimization of cost, by-product resource, poison
Recycling.
The above for those of ordinary skill in the art can according to the technique and scheme of the present invention and technology
Other various corresponding changes and modifications are made in design, and all these change and modification all should belong to the appended right of the present invention
It is required that protection scope.
Claims (3)
1. resourcebility desulfurization denitration demercuration integral process, which is characterized in that using in absorption plant or before additionally plus
Enter the oxidation air oxidation NO for going together in the same direction with flue gas and the mercury in flue gas, generates NO2 And HgO.
2. resourcebility desulfurization denitration demercuration integral process, which is characterized in that in slurry pool before nitrate crystallization is precipitated
Using plaster slurry pump export section absorption tower slurries to gypsum rotational flow station, and gypsum eddy flow overflow slurries in part are imported and are taken off
Sulphur wastewater treatment equipment, or tower slurries will be partially absorbed using existing FGD Wastewater Treatment Process and imported at desulfurization wastewater
It manages device and obtains primary water using desulfurizing waste water processing device to reduce the nitrate concentration of slurry pool of absorption tower slurries, it will
The primary water imports distillation crystallization apparatus evaporative crystallization and obtains nitrate crystallization.
3. resourcebility desulfurization denitration demercuration integral process, which is characterized in that soluble easily in water for desulphurization denitration by-product
Technique, can by the by-product simultaneously crystallize and obtain mixed fertilizer, or using the by-product at different temperatures
Different solubility and it is crystallized respectively, is separated, to obtain pure nitrate agricultural fertilizer, and isolate chloride ion, again
Metal ion crystal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910105962.6A CN109701375A (en) | 2015-03-25 | 2015-03-25 | Resourcebility desulfurization denitration demercuration integral process |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510134825.7A CN105582793A (en) | 2015-03-25 | 2015-03-25 | Resourcelized desulfurization, denitrification and demercuration integrated process |
| CN201910105962.6A CN109701375A (en) | 2015-03-25 | 2015-03-25 | Resourcebility desulfurization denitration demercuration integral process |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510134825.7A Division CN105582793A (en) | 2015-03-25 | 2015-03-25 | Resourcelized desulfurization, denitrification and demercuration integrated process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109701375A true CN109701375A (en) | 2019-05-03 |
Family
ID=55922916
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910105962.6A Pending CN109701375A (en) | 2015-03-25 | 2015-03-25 | Resourcebility desulfurization denitration demercuration integral process |
| CN201510134825.7A Pending CN105582793A (en) | 2015-03-25 | 2015-03-25 | Resourcelized desulfurization, denitrification and demercuration integrated process |
Family Applications After (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510134825.7A Pending CN105582793A (en) | 2015-03-25 | 2015-03-25 | Resourcelized desulfurization, denitrification and demercuration integrated process |
Country Status (1)
| Country | Link |
|---|---|
| CN (2) | CN109701375A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110332558A (en) * | 2019-08-20 | 2019-10-15 | 华中科技大学 | A kind of supercharged oxygen-enriched flue gas desulfurization and denitrification demercuration system |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106582246A (en) * | 2016-12-26 | 2017-04-26 | 合肥天翔环境工程有限公司 | Carbide slag wet-method flue gas simultaneous desulfurization and denitrification process |
| CN110064293B (en) * | 2019-04-30 | 2022-02-11 | 中南大学 | Method for desulfurization, denitrification and demercuration of flue gas |
| CN113041838A (en) * | 2021-05-06 | 2021-06-29 | 昆明理工大学 | Method for cooperatively removing low-concentration sulfur dioxide and mercury in smelting flue gas |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090155149A1 (en) * | 2004-04-09 | 2009-06-18 | Shih-Ger Chang | Method for scavenging mercury |
| CN102350198A (en) * | 2011-07-19 | 2012-02-15 | 中环（中国）工程有限公司 | Flue gas baffling double-slurry pool absorbing tower |
| CN103505997A (en) * | 2013-09-29 | 2014-01-15 | 环境保护部华南环境科学研究所 | Smoke and multi-pollutant efficient synergistic purification method and application thereof |
| CN103638792A (en) * | 2013-12-17 | 2014-03-19 | 张继惟 | LSCO-AS (low-temperature selective catalytic-oxidation-as simulating system) technology system for purifying oxygen-enriched combustion smoke |
| CN103721551A (en) * | 2014-01-26 | 2014-04-16 | 王骞 | Boiler flue gas desulfurization, denitration and mercury removal integrated purification device |
| CN103801178A (en) * | 2014-03-06 | 2014-05-21 | 汤宁 | Smoke purification device and method with integration of desulfuration, denitration, dust removal and mercury removal |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070149394A1 (en) * | 2005-12-22 | 2007-06-28 | Foster Wheeler Energy Corporation | Catalyst, a method of using a catalyst, and an arrangement including a catalyst, for controlling NO and/or CO emissions from a combustion system without using external reagent |
| CN101306322B (en) * | 2008-02-22 | 2011-07-13 | 北京博奇电力科技有限公司 | Integrative coordinated desulfurization, denitration, demercuration device and technique using spray bubbling method |
| CN101310834B (en) * | 2008-02-25 | 2011-02-23 | 北京博奇电力科技有限公司 | Desulfurization, denitration, demercuration technique using gas-liquid contact step oxidation process |
| CN101259372B (en) * | 2008-04-29 | 2011-06-29 | 刘海清 | Flue gas desulfurization denitration dust-removing integrated technique |
| CN101816888A (en) * | 2010-05-14 | 2010-09-01 | 孙厚杰 | Wet flue gas desulfurization absorption tower for power plant |
| CN102553428A (en) * | 2012-01-10 | 2012-07-11 | 华北电力大学（保定） | Absorption tower for desulfurization and denitrification combined with oxidant in forward-flow and back-flow spraying and method |
| CN102824843B (en) * | 2012-08-28 | 2014-07-02 | 西安交通大学 | Combined removal device and method for sulphur, mercury and nitrate in smoke |
| CN103977702B (en) * | 2014-05-16 | 2016-01-27 | 南京师范大学 | A kind of circulating fluid bed flue-gas desulfurizing denitration demercuration integrated apparatus and method |
-
2015
- 2015-03-25 CN CN201910105962.6A patent/CN109701375A/en active Pending
- 2015-03-25 CN CN201510134825.7A patent/CN105582793A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090155149A1 (en) * | 2004-04-09 | 2009-06-18 | Shih-Ger Chang | Method for scavenging mercury |
| CN102350198A (en) * | 2011-07-19 | 2012-02-15 | 中环（中国）工程有限公司 | Flue gas baffling double-slurry pool absorbing tower |
| CN103505997A (en) * | 2013-09-29 | 2014-01-15 | 环境保护部华南环境科学研究所 | Smoke and multi-pollutant efficient synergistic purification method and application thereof |
| CN103638792A (en) * | 2013-12-17 | 2014-03-19 | 张继惟 | LSCO-AS (low-temperature selective catalytic-oxidation-as simulating system) technology system for purifying oxygen-enriched combustion smoke |
| CN103721551A (en) * | 2014-01-26 | 2014-04-16 | 王骞 | Boiler flue gas desulfurization, denitration and mercury removal integrated purification device |
| CN103801178A (en) * | 2014-03-06 | 2014-05-21 | 汤宁 | Smoke purification device and method with integration of desulfuration, denitration, dust removal and mercury removal |
Non-Patent Citations (1)
| Title |
|---|
| 林文孚: "《单位机组热力设备运行》", 30 September 2008, 中国水利水电出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110332558A (en) * | 2019-08-20 | 2019-10-15 | 华中科技大学 | A kind of supercharged oxygen-enriched flue gas desulfurization and denitrification demercuration system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105582793A (en) | 2016-05-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Li et al. | Summary of research progress on industrial flue gas desulfurization technology | |
| CN102015070B (en) | System for treating discharge gas and method of removing mercury from discharge gas | |
| CN100360212C (en) | Waste gas control method by removing sulfur dioxide for resource utilization | |
| JP5554162B2 (en) | Mercury treatment system in exhaust gas | |
| US10247414B2 (en) | Coal-fired boiler exhaust gas treatment apparatus and coal-fired boiler exhaust gas treatment method | |
| CN109701375A (en) | Resourcebility desulfurization denitration demercuration integral process | |
| CN103499098B (en) | A kind of high concentration organic waste liquid burning equipment and technique | |
| CN108310938A (en) | By dechlorination to control the method and system of desulfurization wastewater discharge | |
| Carpenter | Low water FGD technologies | |
| CN102350208A (en) | Flue gas absorbent which simultaneously has functions of desulphurization and denitration and preparation method and application thereof | |
| Zhou et al. | Review on occurrence, speciation, transition and fate of sulfur in typical ultra-low emission coal-fired power plants | |
| CN106178865B (en) | Industrial furnace smoke heavy metal and the purification of fluorine chlorine sulphur nitre and resource utilization method | |
| CN104524935A (en) | Single-tower type double-circulation sprinkling composite absorption device and method | |
| Ma et al. | Synthesis, properties and application of double salt (NH4) 2Mg (SO4) 2· 6H2O in wet magnesium-ammonia FGD process | |
| CN103100294A (en) | Method for removing oxynitride from flue gas through ozone oxidation method | |
| CN102188889B (en) | Device and method for combined removal of sulphur dioxide (SO2), nitrogen oxide (NOX) and mercury from fume | |
| Liu et al. | Advanced Oxidative Removal of Nitric Oxide from Flue Gas by Homogeneous Photo‐Fenton in a Photochemical Reactor | |
| CN106268283B (en) | The method of cement kiln flue gas removing heavy metal and sulphur nitre pollutant and resource utilization | |
| CN104587819A (en) | Fixing method of carbon dioxide in flue gas of municipal solid waste incinerator | |
| CN107051173A (en) | One kind utilizes SO in carbide slag removing boiler smoke3Structure and method | |
| CN103551015A (en) | Sulfur dioxide absorbent prepared from two-alkali salt slurry | |
| CN106823772A (en) | Desulfuration in furnace synergist and desulfurizing agent | |
| CN111137964A (en) | Coal-fired boiler ammonia desulfurization slurry dechlorination treatment process | |
| CN101623591A (en) | Desulfurization and denitrification oxidation process of single-stage catalytic reduction absorption method | |
| JP2009131726A (en) | Method of treating flue gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190503 |