CN103861439A - Method for simultaneously desulfurizing, denitrating and purifying flue gas - Google Patents

Method for simultaneously desulfurizing, denitrating and purifying flue gas Download PDF

Info

Publication number
CN103861439A
CN103861439A CN201410113793.8A CN201410113793A CN103861439A CN 103861439 A CN103861439 A CN 103861439A CN 201410113793 A CN201410113793 A CN 201410113793A CN 103861439 A CN103861439 A CN 103861439A
Authority
CN
China
Prior art keywords
flue gas
ammonia
active carbon
ammonium sulfate
absorption
Prior art date
Application number
CN201410113793.8A
Other languages
Chinese (zh)
Inventor
曾子平
刘成
周锡飞
Original Assignee
云南亚太环境工程设计研究有限公司
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by 云南亚太环境工程设计研究有限公司 filed Critical 云南亚太环境工程设计研究有限公司
Priority to CN201410113793.8A priority Critical patent/CN103861439A/en
Publication of CN103861439A publication Critical patent/CN103861439A/en

Links

Classifications

    • Y02A50/2344
    • Y02A50/2349
    • Y02P20/153

Abstract

The invention discloses a method for simultaneously desulfurizing, denitrating and purifying flue gas and belongs to the field of flue gas purification. The method comprises the following steps: spraying the flue gas at the temperature of 50-90 DEG C by using ammonia absorption liquid to obtain a solution, and aerating and oxidizing the solution to obtain an ammonium sulfate solution; exchanging heat between the obtained flue gas and the original flue gas, heating to 120-350 DEG C, and supplementing ammonium hydroxide; converting NO and NO2 in the flue gas into N2 by addition or non-addition of an activated carbon material of a catalyst; performing reaction on the remaining SO2, ammonia and water vapor to generate ammonium sulfate; adsorbing mercury, dioxin, furan, a volatile organic compound, ammonia sol and other trace toxic substances by activated carbon; and regenerating the activated carbon after absorption and adsorption by using washing and heating methods. The method has the advantages that the process is simple and convenient, and the desulfurizing and denitrating efficiency is high; various toxic substances and fine particles in the flue gas can be adsorbed, a good prevention effect on PM2.5 pollution of industrial flue gas is achieved, ammonium sulfate and ammonium nitrate fertilizer byproducts are obtained, and resources can be recycled. The method can be applied to purification of sulfur-containing and nitrate-containing flue gas in the fields of boilers, metallurgy, chemical industry, thermoelectricity and garbage incineration power generation.

Description

A kind of method of while desulphurization denitration purifying smoke

Technical field:

The invention belongs to flue gases purification field, be specifically related to a kind of method of while desulphurization denitration purifying smoke.

Background technology:

Along with increasingly sharpening of environmental pollution, country has listed air contaminant treatment in emphasis prevention and control target, especially sulphur and the nitrogen oxide index most important thing in Air Pollution Control especially.If with respectively desulphurization denitrations of two covering devices, not only floor space is large, and investment, management, operating cost are also high.In recent years countries in the world especially industrially developed country all in succession carried out the research and development of desulfurization removing nitric technology simultaneously.Oneself becomes simultanously desulfurizing and denitrification purification treatment technology various countries and controls the research and development focus of smoke pollution.

Desulphurization denitration technology refers in a process the SO in flue gas simultaneously 2and NO xthe technology simultaneously removing.According to the process of processing, can be divided into two large classes: the one, while desulphurization denitration technology in stove combustion process.The common feature of these class methods is to reduce the generation of NO by control combustion temperature, utilizes calcium enhancer to absorb the SO producing in combustion process simultaneously 2, control NO and SO 2discharge.As CFBC method, sodium matter sorbent injection method etc.; Another kind of is flue gas combined desulfurization and denitration technology after burning, and these class methods are to grow up on the basis of flue gas desulfurization method, and existing while desulphurization denitration technology mainly contains dry method flue gas desulphurization denitration technology and wet flue gas desulphurization denitration technology simultaneously simultaneously.Wherein, dry method flue gas simultaneously desulphurization denitration technology comprise LILAC method, NOxSO method, activated carbon method, recirculating fluidized bed method, plasma method; Wet flue gas simultaneously desulphurization denitration technology comprises oxidation absorption process and wet type Absorption via Chemical Complexation.But said method exists technology complexity, severe reaction conditions, desulfurization off sulfide effect is poor and operating cost is high shortcoming.Particularly a large amount of catalysts selective reduction denitration technology (SCR) or the non-catalytic reduction denitration technologies (SNCR) that adopt of China carry out denitration at present, carry out sulfur removal technology with limestone-gypsum method again, this method exists that cost of investment is high, operating cost is high, produce a large amount of by-product desulfurated plasters, post-processed is difficulty comparatively simultaneously.

Summary of the invention:

The object of this invention is to provide a kind of technology easy, effect is remarkable, the method for desulphurization denitration purifying smoke when operating cost is low.

The method of a kind of while desulphurization denitration purifying smoke of the present invention, this comprises the following steps:

A. 50~90 DEG C of sulfur-bearings are carried out to more than 95% SO of mol ratio in ammonia wet absorption flue gas containing smoke of gunpowder gas in ammonia absorber (2) 2, gained solution obtains ammonium sulfate after the oxidation of aeration oxidator (4) aeration;

B. the flue gas that contains nitrogen oxide, ammonia, a small amount of sulfur dioxide and other impurity after preliminary purification is heated to, after 120 DEG C~350 DEG C, add ammoniacal liquor according to nitrogen oxides in effluent and ammonia content at flue gas heat-exchange unit (1) the former flue gas heat exchange of 200~1100 DEG C; By adding or do not add the active carbon absorbent charcoal material of catalyst, make NO and NO in flue gas at charcoal trap (9) 2be converted into N 2, part NO 2in the situation that existing, water vapour is converted into NH with ammonia 4nO 3; Reaction equation is:

4NO+O 2+4NH 3—4N 2+6H 20

2NO 2+4NH 3+O 2—3N 2+6H 2O

3NO 2+2NH 3+H 2O—2NH 4NO 3+NO

Residue SO 2under active carbon effect, generate ammonium sulfate with ammonia, steam; Reaction equation is:

2SO 2+O 2+2H 2O→2H 2SO 4

NH 3+H 2SO 4→NH 4HSO 4

NH 3+H 2SO 4→(NH 4) 2SO 4

C. mercurous, the bioxin of flue gas institute, furans, volatile organic matter, ammonia aerosols and other micro-harmful toxic matters are by charcoal absorption; Active carbon absorb absorption after in regenerating active carbon tower (11) adopt washing or heat method regenerate.

The ammonia in flue gas and the nitrous oxides concentration that in above-mentioned b step, enter charcoal trap (9) active carbon layer are controlled at NH 3/ NOx mol ratio is 0.8~1.1; Absorbent charcoal material is the one in active carbon, activated coke, NACF; Catalyst is Mn(NO 3) 2, Fe(NO 3) 2, Cr(NO 3) 2, CuO, V 2o 5in one or both.

Above-mentioned steps absorbs NO xand SO 2after the desulfurization absorption liquid concentrate drying of gas, be ammonium sulfate and ammonium nitrate fertilizer.

The present invention's equipment used is existing known equipment.The absorbent charcoal material that the present invention is used and catalyst are that market is bought.

Beneficial effect of the present invention is:

(1) desulphurization denitration can be completed simultaneously, desulfuration efficiency>=99%, denitration efficiency>=85%, exhausted gas nitrogen oxide < 100mg/m 3, sulfur dioxide concentration < 50mg/m 3, meet national relevant emission standards.

(2) can remove that flue gas institute is mercurous, bioxin, furans, heavy metal, volatile organic matter and other micro-harmful toxic matters, and can adsorbed gas colloidal sol, PM2.5 particle, flue gas strong adaptability, wide application, is specially adapted to contain smoke of gunpowder gas containing the sulfur-bearing of a small amount of harmful toxic matter.

(3) process identical exhaust gas volumn, the present invention compares SNCR method+desulfurization of gypsum method, cost ± 25%, and running cost reduces ± 40%.

(4) because the present invention is in denitration and two stages of desulfurization, use same ammoniacal liquor raw material, in the time that construction investment is produced, can share a set of ammonia supply equipment; Separately, in the denitration stage, can absorb ammonia unnecessary in desulfurization stage, the consumption of raw material is reduced greatly, operation maintenance cost reduces.

(5) main byproduct is the ammonium sulfate fertilizer that contains a small amount of ammonium nitrate, has realized the object of recycling economy.

Brief description of the drawings:

Accompanying drawing is process chart schematic diagram of the present invention.Mark in figure:

1, flue gas heat exchange radiator; 2, ammonia absorber; 3, sprayer-washer; 4, aeration oxidator; 5, circulating pump; 6, air blast pump; 7, ammoniacal liquor station; 8, sedimentation filter thickener; 9, charcoal trap; 10, active carbon storehouse; 11, regenerating active carbon tower; 12, baker.

Detailed description of the invention:

Below in conjunction with accompanying drawing, the present invention is made to specific description.

In embodiment, equipment used is existing known equipment; Absorbent charcoal material used and catalyst are that market is bought.In embodiment, method used is with the description of summary of the invention part.

Embodiment mono-:

By the sulfur-bearing of 1100 DEG C containing smoke of gunpowder gas by desulfurization fume heat exchange be cooled to 90 DEG C in flue gas heat-exchange unit 1 after absorbing with ammonia, enter ammonia absorber 2, with the ammonium sulfate contact of adding ammoniacal liquor under sprayer-washer 3 top sprays, pass through spray washing, wash away the dust in flue gas, flue gas in this process because adiabatic evaporation is cooling, the simultaneously SO in flue gas 2be absorbed the absorption liquid absorption that liquid circulating pump 5 is sent here.Absorption liquid falls into aeration oxidator 4 subsequently by reflux line, blasting air aeration by air blast pump 6 is ammonium sulfate by sub-salt (ammonium sulfite and ammonium bisulfite) solution oxide, after 5 pressurizations of absorption liquid circulating pump, send into sprayer-washer 3 spray equipments, continue circulated sprinkling and absorb; The shunting of absorption liquid that system increases enters sedimentation filter thickener 8, and ammonium sulfate concentrates because of the evaporation of moisture, and concentration improves gradually, and its heat of evaporation is supplied with by fume afterheat, then enters following process and become solid ammonium sulfate.Along with the carrying out of absorption process, liquid absorption element constantly changes, and absorbability is reduced.For keeping absorption efficiency, palpus is constantly supplementary, and new desulfurizing agent---ammoniacal liquor is regenerated absorbent.Supplement absorbent ammoniacal liquor by ammonia station 7.

Flue gas through the preliminary purification of ammonia absorber portion is heated to 350 DEG C by flue gas heat-exchange unit 1, enters charcoal trap 9 bottoms, according to NO in flue gas xcontent sprays into a small amount of ammoniacal liquor at tower side lower part, controls NH in flue gas 3/ NOx mol ratio is 1.0, and flue gas is through adding Mn(NO 3) 2or Fe(NO 3) 2or Cr(NO 3) 2the activated coke layer of catalyst, in flue gas, NOx and ammonia are converted into N 2; Residue SO 2generate ammonium sulfate with ammonia; Contained aerosol, other micro-harmful toxic matter and PM2.5 particle are by charcoal absorption, and after purifying, flue gas is discharged from charcoal trap 9 tops, enters air flue emission.

Activated coke after absorption transports through 9 bottoms, absorption tower, enters regenerating active carbon tower 11 and is heated to 400 DEG C and regenerates, and is then added by top, absorption tower, forms uninterrupted regeneration, and the activated coke of loss is added through active carbon storehouse 10.

Embodiment bis-:

Certain sulfur-bearing of 200 DEG C is contained to smoke of gunpowder gas by absorbing rear desulfurization fume in flue gas heat-exchange unit 1 heat exchange and be cooled to 50 DEG C with ammonia, enter ammonia absorber 2, with the ammonia spirit spray washing under spray absorber 3 top sprays, wash away the dust in flue gas, and carry out desulfurization.Solution after desulfurization generates ammonium sulfate through air aeration oxidation in aeration oxidator 4, after sedimentation filter thickener 8, produces ammonium sulfate fertilizer; Flue gas after desulfurization is through flue gas heat-exchange unit 1 heat exchange to 120 DEG C, according to NO in flue gas xcontent sprays into a small amount of ammoniacal liquor in pipeline, controls NH in flue gas 3/ NOx mol ratio is 0.8, enters charcoal trap 9 bottoms, and flue gas is through adding CuO and V 2o 5the active carbon layer of catalyst carries out deep purifying.In flue gas, NOx and ammonia are converted into N 2; Residue SO 2generate ammonium sulfate with ammonia; Bioxin, furans, volatile organic matter, other micro-harmful toxic matters and PM2.5 particle are by charcoal absorption, and after purifying, flue gas is discharged from top, absorption tower, enters air flue emission.

Active carbon after absorption transports through 9 bottoms, absorption tower, enters regenerating active carbon tower 11 and carries out regenerated from washing, then drying device 12) dry after, added by charcoal trap 9 tops, form uninterrupted regeneration,, the active carbon of loss is added through active carbon storehouse 10.Cleaning solution enters after 8 filtrations of sedimentation filter thickener, sneaks in ammonia absorber portion ammonium sulfate and produces chemical fertilizer.

Embodiment tri-:

By 900 DEG C of certain mercurous metallurgical gas by desulfurization fume after absorbing with ammonia in flue gas heat-exchange unit 1 heat exchange and be cooled to 75 DEG C, enter ammonia absorber 2, with the ammonium sulfate contact of adding ammoniacal liquor under sprayer-washer 3 top sprays, pass through spray washing, wash away the dust in flue gas, flue gas in this process because adiabatic evaporation is cooling, the simultaneously SO in flue gas 2be absorbed the absorption liquid absorption that liquid circulating pump 5 is sent here.Absorption liquid falls into aeration oxidator 4 subsequently by reflux line, blasting air aeration by air blast pump 6 is ammonium sulfate by sub-salt (ammonium sulfite and ammonium bisulfite) solution oxide, after 5 pressurizations of absorption liquid circulating pump, send into sprayer-washer 3 spray equipments, continue circulated sprinkling and absorb; The absorption liquid shunting that system increases enters sedimentation filter thickener 8, the heavy metal dissolving in decanting zone regulator solution pH value sedimentation, after filtration, concentrate, ammonium sulfate concentrates because of the evaporation of moisture, concentration improves gradually, its heat of evaporation is supplied with by fume afterheat, then enters following process and become solid ammonium sulfate.Flue gas after desulfurization is through flue gas heat-exchange unit 1 heat exchange to 270 DEG C, according to NO in flue gas xcontent sprays into ammoniacal liquor in pipeline, controls NH in flue gas 3/ NOx mol ratio is 1.1, enters charcoal trap 9 bottoms, and flue gas carries out deep purifying through not adding catalyst activity charcoal fiber.In flue gas, NOx and ammonia are converted into N 2; Residue SO 2generate ammonium sulfate with ammonia; Mercury subparticle, ammonia aerosols and other PM2.5 particles are by charcoal absorption, and after purifying, flue gas is discharged from charcoal trap 9 tops, enters air flue emission.

NACF after absorption transports through bottom, absorption tower, enters regenerating active carbon tower 11 and carries out regenerated from washing, after then drying device 12 is dried, is added by charcoal trap 9 tops, and the NACF of loss is added through active carbon storehouse 10.Cleaning solution enters after 8 filtrations of sedimentation filter thickener, sneaks in ammonia absorber portion ammonium sulfate and produces chemical fertilizer.After charcoal absorption a period of time, as emission mercury content reaches 80% of discharge standard setting, removable parts active carbon, the mercurous NACF under changing send the business processes of processing qualification.

Practical application shows: the present invention can not only complete desulphurization denitration simultaneously, and desulfuration efficiency>=99%, denitration efficiency>=85%, exhausted gas nitrogen oxide < 100mg/m 3, sulfur dioxide concentration < 50mg/m 3, meet national relevant emission standards.The present invention compares SNCR method+desulfurization of gypsum method, cost ± 25%, and running cost reduces ± 40%.

Claims (3)

1. a method for while desulphurization denitration purifying smoke, this comprises the following steps to it is characterized in that method:
A. 50~90 DEG C of sulfur-bearings are carried out to more than 95% SO of mol ratio in ammonia wet absorption flue gas containing smoke of gunpowder gas in ammonia absorber (2) 2, gained solution obtains ammonium sulfate after the oxidation of aeration oxidator (4) aeration;
B. the flue gas that contains nitrogen oxide, ammonia, a small amount of sulfur dioxide and other impurity after preliminary purification is heated to, after 120 DEG C~350 DEG C, add ammoniacal liquor according to nitrogen oxides in effluent and ammonia content at flue gas heat-exchange unit (1) the former flue gas heat exchange of 200~1100 DEG C; By adding or do not add the active carbon absorbent charcoal material of catalyst, make NO and NO in flue gas at charcoal trap (9) 2be converted into N 2, part NO 2in the situation that existing, water vapour is converted into NH with ammonia 4nO 3; Reaction equation is:
4NO+O 2+4NH 3—4N 2+6H 20
2NO 2+4NH 3+O 2—3N 2+6H 2O
3NO 2+2NH 3+H 2O—2NH 4NO 3+NO
Residue SO 2under active carbon effect, generate ammonium sulfate with ammonia, steam; Reaction equation is:
2SO 2+O 2+2H 2O→2H 2SO 4
NH 3+H 2SO 4→NH 4HSO 4
NH 3+H 2SO 4→(NH 4) 2SO 4
C. mercurous, the bioxin of flue gas institute, furans, volatile organic matter, ammonia aerosols and other micro-harmful toxic matters are by charcoal absorption; Active carbon absorb absorption after in regenerating active carbon tower (11) adopt washing or heat method regenerate.
2. the method for a kind of while desulphurization denitration purifying smoke according to claim 1, is characterized in that the ammonia in flue gas and the nitrous oxides concentration that in b step, enter charcoal trap (9) active carbon layer are controlled at NH 3/ NOx mol ratio is 0.8~1.1; Absorbent charcoal material is the one in active carbon, activated coke, NACF; Catalyst is Mn(NO 3) 2, Fe(NO 3) 2, Cr(NO 3) 2, CuO, V 2o 5in one or both.
3. the method for a kind of while desulphurization denitration purifying smoke according to claim 1, is characterized in that: absorb NO xand SO 2after the desulfurization absorption liquid concentrate drying of gas, be ammonium sulfate and ammonium nitrate fertilizer.
CN201410113793.8A 2014-03-25 2014-03-25 Method for simultaneously desulfurizing, denitrating and purifying flue gas CN103861439A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201410113793.8A CN103861439A (en) 2014-03-25 2014-03-25 Method for simultaneously desulfurizing, denitrating and purifying flue gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201410113793.8A CN103861439A (en) 2014-03-25 2014-03-25 Method for simultaneously desulfurizing, denitrating and purifying flue gas

Publications (1)

Publication Number Publication Date
CN103861439A true CN103861439A (en) 2014-06-18

Family

ID=50900811

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201410113793.8A CN103861439A (en) 2014-03-25 2014-03-25 Method for simultaneously desulfurizing, denitrating and purifying flue gas

Country Status (1)

Country Link
CN (1) CN103861439A (en)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104386653A (en) * 2014-10-24 2015-03-04 云南亚太环境工程设计研究有限公司 Method for producing liquid sulfur dioxide by using sulfur-containing flue gas
CN104525116A (en) * 2014-12-31 2015-04-22 上海克硫环保科技股份有限公司 Desulfurization and denitrification modified active coke and preparation method thereof
CN105080265A (en) * 2015-02-04 2015-11-25 崔怀奇 Industrial tail gas recovery and recycle major cycle technology
CN105214480A (en) * 2015-11-13 2016-01-06 朱忠良 A kind of flue gas purifying technique
CN105289492A (en) * 2015-11-17 2016-02-03 东华大学 Multifunctional desulfurization, denitrification, demercuration adsorbent and preparation and application thereof
CN105771576A (en) * 2016-03-24 2016-07-20 宁波德纳希环保科技有限公司 Process of utilizing modified activated carbon to remove dioxin
CN106492822A (en) * 2016-09-28 2017-03-15 北京科技大学 Efficient cryogenic removes NO<sub>x</sub>、Hg<sup>0</sup>Preparation method with the activated coke based specimen of VOCs
CN106621773A (en) * 2016-12-30 2017-05-10 中南大学 Ammonia-carbon combined desulfurization and denitration method for sintering flue gas
CN107846900A (en) * 2015-06-19 2018-03-27 地球科学实验室 The chelating alkali product handled for water based systems and the method for preparing alkali product
CN108479369A (en) * 2018-04-24 2018-09-04 中国石油化工股份有限公司 A kind of ultra-clean discharge ammonia desulfuration equipment and technique
CN109592647A (en) * 2018-12-17 2019-04-09 山东大学 Sulphur/nitrate iron-charcoal reduction prepares sulphur and recycles desulfurization/nitre agent technique
US10807889B2 (en) 2015-06-19 2020-10-20 Earth Science Laboratories Chelating base product for use in water-based system treatments

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5466427A (en) * 1993-07-14 1995-11-14 Cabot Corporation Catalysis and treatment of gases with the catalysts
EP0702592A1 (en) * 1993-06-09 1996-03-27 Linde Ag Method of removing hcn from mixtures of gases and a catalyst for decomposing hcn
CN200957341Y (en) * 2006-06-06 2007-10-10 施耀 Wet smoke desulfurizer by ammonia method
CN101785969A (en) * 2010-03-03 2010-07-28 王向明 Method of flue gas purification and system thereof
CN202224048U (en) * 2011-09-14 2012-05-23 中冶赛迪工程技术股份有限公司 Sintering flue gas treatment device
CN202460474U (en) * 2012-01-19 2012-10-03 大连贝斯特环境工程设备有限公司 Integral desulfurization and denitration complete device by catalytic reduction ammonia method for small and medium boilers
CN203075823U (en) * 2012-10-10 2013-07-24 住友重机械工业株式会社 Waste gas treatment device
CN203139884U (en) * 2012-10-29 2013-08-21 住友重机械工业株式会社 Exhaust-gas treatment apparatus

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0702592A1 (en) * 1993-06-09 1996-03-27 Linde Ag Method of removing hcn from mixtures of gases and a catalyst for decomposing hcn
US5466427A (en) * 1993-07-14 1995-11-14 Cabot Corporation Catalysis and treatment of gases with the catalysts
CN200957341Y (en) * 2006-06-06 2007-10-10 施耀 Wet smoke desulfurizer by ammonia method
CN101785969A (en) * 2010-03-03 2010-07-28 王向明 Method of flue gas purification and system thereof
CN202224048U (en) * 2011-09-14 2012-05-23 中冶赛迪工程技术股份有限公司 Sintering flue gas treatment device
CN202460474U (en) * 2012-01-19 2012-10-03 大连贝斯特环境工程设备有限公司 Integral desulfurization and denitration complete device by catalytic reduction ammonia method for small and medium boilers
CN203075823U (en) * 2012-10-10 2013-07-24 住友重机械工业株式会社 Waste gas treatment device
CN203139884U (en) * 2012-10-29 2013-08-21 住友重机械工业株式会社 Exhaust-gas treatment apparatus

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
蒋文举: "《烟气脱硫脱硝技术手册》", 31 December 2012 *

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104386653A (en) * 2014-10-24 2015-03-04 云南亚太环境工程设计研究有限公司 Method for producing liquid sulfur dioxide by using sulfur-containing flue gas
CN104525116A (en) * 2014-12-31 2015-04-22 上海克硫环保科技股份有限公司 Desulfurization and denitrification modified active coke and preparation method thereof
CN105080265A (en) * 2015-02-04 2015-11-25 崔怀奇 Industrial tail gas recovery and recycle major cycle technology
CN105080265B (en) * 2015-02-04 2020-10-16 茏源(北京)环保科技有限公司 Industrial tail gas recycling large-cycle process
CN107846900A (en) * 2015-06-19 2018-03-27 地球科学实验室 The chelating alkali product handled for water based systems and the method for preparing alkali product
US10807889B2 (en) 2015-06-19 2020-10-20 Earth Science Laboratories Chelating base product for use in water-based system treatments
CN105214480A (en) * 2015-11-13 2016-01-06 朱忠良 A kind of flue gas purifying technique
CN105289492B (en) * 2015-11-17 2019-07-23 东华大学 A kind of multi-functional desulfurization denitration demercuration adsorbent and its preparation and application
CN105289492A (en) * 2015-11-17 2016-02-03 东华大学 Multifunctional desulfurization, denitrification, demercuration adsorbent and preparation and application thereof
CN105771576A (en) * 2016-03-24 2016-07-20 宁波德纳希环保科技有限公司 Process of utilizing modified activated carbon to remove dioxin
CN105771576B (en) * 2016-03-24 2018-09-11 宁波德纳希环保科技有限公司 A kind of technique removing bioxin using modified activated carbon
CN106492822A (en) * 2016-09-28 2017-03-15 北京科技大学 Efficient cryogenic removes NO<sub>x</sub>、Hg<sup>0</sup>Preparation method with the activated coke based specimen of VOCs
CN106621773A (en) * 2016-12-30 2017-05-10 中南大学 Ammonia-carbon combined desulfurization and denitration method for sintering flue gas
CN106621773B (en) * 2016-12-30 2019-11-26 中南大学 A kind of sintering flue gas ammonia charcoal combined desulfurization and denitration method
CN108479369A (en) * 2018-04-24 2018-09-04 中国石油化工股份有限公司 A kind of ultra-clean discharge ammonia desulfuration equipment and technique
CN109592647B (en) * 2018-12-17 2020-01-10 山东大学 Process for preparing sulfur and recovering desulfurizing/nitre agent by sulfur/nitrate iron-carbon reduction
WO2020124655A1 (en) * 2018-12-17 2020-06-25 山东大学 Process for preparing sulfur by means of sulfate/nitrate iron-carbon reduction and recovering desulfurization/denitrification agent
CN109592647A (en) * 2018-12-17 2019-04-09 山东大学 Sulphur/nitrate iron-charcoal reduction prepares sulphur and recycles desulfurization/nitre agent technique

Similar Documents

Publication Publication Date Title
US7514053B2 (en) Method for removing sulfur dioxide, mercury, and nitrogen oxides from a gas stream
CA2675503C (en) Use of so2 from flue gas for acid wash of ammonia
AU2011259875B2 (en) Air pollution control system and method
US8877149B2 (en) Combustion flue gas NOx treatment
CN103933838B (en) In coal, chlorine element circular utilizes the device and method realizing pollutant combined removal
CN101745305B (en) Method for removing various gaseous pollutants from smoke gas
CN1331571C (en) Flue gas hydrargyrum-removing method by catalytic oxidation
CN102247750B (en) Method for simultaneously desulfurizing and denitrifying flue gas by ozone catalytic oxidation process
EP2044997B1 (en) Apparatus for removing of trace of toxic substance from exhaust gas and method of operating the same
CN105056749A (en) System and method for removing nitric oxides and sulfur oxides in flue gas simultaneously
CN103706238B (en) System and method for removing SO2, NO and Hg in smoke on the basis of heterogeneous Fenton
CN103230733B (en) The device of a kind of liquid phase catalytic oxidation flue gas desulfurization and denitrification integration and technique
CN101352644B (en) Wet flue gas denitration technique for nitrite recovery
CN101279185B (en) Gas phase oxidation-liquid phase reduction method for absorbing and removing nitrous oxides in exhaust air
CN1843575B (en) Method and apparatus for optic catalytic oxidizing, desulfurizing and denitrifying flue gas simultaneously
CN102512927B (en) Integrated flue gas desulfurizing and denitrating purification system and purification technology for same
AU2011259876B2 (en) Exhaust gas treatment system and method
CN1923341A (en) Device and method for coal-burning boiler fume ozone oxidation and simultaneous desulfurization and denitrification
CN102489129B (en) Industrial flue gas purification, desulfurization and denitrification integrated device and working method thereof
CN102716648B (en) Method for automatically controlling desulphurization and denitration by flue gas based on pH value and ORP value and apparatus thereof
US20070154374A1 (en) Method for removing sulfur dioxide and other acid gases, mercury, and nitrogen oxides from a gas stream with the optional production of ammonia based fertilizers
CN203437036U (en) Sintering fume desulfurization and denitrification device
CN103007679B (en) Flue gas cleaning system capable of switching pollutant desorption technology and adsorbent regeneration technology and method thereof
CN103239985B (en) Efficient fuel coal flue gas desulfurizing and hydrargyrum-removing method and device thereof
US8496895B2 (en) Exhaust gas treating apparatus and treating method for carbon dioxide capture process

Legal Events

Date Code Title Description
PB01 Publication
C06 Publication
SE01 Entry into force of request for substantive examination
C10 Entry into substantive examination
RJ01 Rejection of invention patent application after publication

Application publication date: 20140618

C12 Rejection of a patent application after its publication