CN103292604A - Flue gas afterheat-recycling, desulfurizing and denitrifying method and device - Google Patents

Flue gas afterheat-recycling, desulfurizing and denitrifying method and device Download PDF

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Publication number
CN103292604A
CN103292604A CN2012100500751A CN201210050075A CN103292604A CN 103292604 A CN103292604 A CN 103292604A CN 2012100500751 A CN2012100500751 A CN 2012100500751A CN 201210050075 A CN201210050075 A CN 201210050075A CN 103292604 A CN103292604 A CN 103292604A
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China
Prior art keywords
flue gas
temperature
absorption liquid
air
absorption tower
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CN2012100500751A
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Chinese (zh)
Inventor
郜建松
孙志钦
孟庆凯
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中国石油化工股份有限公司
中国石化集团洛阳石油化工工程公司
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Priority to CN2012100500751A priority Critical patent/CN103292604A/en
Publication of CN103292604A publication Critical patent/CN103292604A/en

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    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02EREDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00Combustion technologies with mitigation potential
    • Y02E20/34Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00Technologies related to metal processing
    • Y02P10/25Process efficiency

Abstract

The invention discloses a flue gas afterheat-recycling, desulfurizing and denitrifying method and a flue gas afterheat-recycling, desulfurizing and denitrifying device. The flue gas afterheat-recycling, desulfurizing and denitrifying method comprises the following steps: SOX-containing and NOX-containing flue gas at the temperature of 300-360 DEG C enters an air preheater and exchanges heat with air at the temperature of 60-70 DEG C; the flue gas cooled to 150-220 DEG C enters an absorption tower to be in contact with absorption liquid; the absorption liquid transfers heat to the high-temperature end of a heat pipe; and air exchanges heat with the low-temperature end of the heat pipe and is heated to 60-70 DEG C. By the flue gas afterheat-recycling, desulfurizing and denitrifying method, the heat recycling efficiency is high, and acid dew point corrosion and harmful gas emission are reduced.

Description

A kind of flue gas waste heat recovery desulfurization denitration method and device
Technical field
The present invention relates to the method that the used a kind of flue gas waste heat recovery process synchronized desulfuring and denitrifying of petroleum refining, petrochemical industry tubular heater purifies.
Background technology
Tubular heater is the big power consumer of petroleum refining and petroleum chemical industry process units, Fuel Consumption occupies sizable ratio in plant energy consumption: at least 20%~30%, at most 80%~90%, therefore reclaim in the flue gas of heating furnace waste heat for reduce Fuel Consumption, reducing production costs has great significance.On the other hand, along with the increase of the mankind to energy demand, the SO that the heating furnace fuel combustion causes X, NO XIncrease day by day with the discharge capacity of flue dust.China has since nineteen ninety-five become SO XThe country of discharge capacity maximum and acid rain serious area, restriction pollutant emission, protection environment, maintenance sustainable development have become the fundamental state policy of China.Generally adopt air preheater to carry out the recovery of fume afterheat on the industrial applications at present, employing flue gas desulphurization system, flue gas denitrification system and flue gas cleaner remove the SO in the flue gas X, NO XAnd flue dust, but these flue gas processing devices all are independent the settings, and heat energy utilization can not be complementary each other, exists waste heat recovery efficient low, and floor space is big, one-time investment expense height, problems such as acid dew piont corrosion easily take place in equipment.Further optimize heat exchange process, realize the heat energy complementation between the purification of flue gas waste heat recovery and desulphurization denitration, thereby simplified apparatus structure, reduce the process units one-time investment, improve waste heat recovery efficient, minimizing equipment acid dew piont corrosion is the direction that the Petrochemical Enterprises tubular heater is further carried out " energy-saving and emission-reduction " work.
Chinese patent CN101648110A discloses a kind of " waste-heat recovery device with function of fuel gas purification ", comprises water jacket, purifying box and flue three big parts, adds to purify medicine in the water of purifying box, and flue gas just can realize removing the SO in the flue gas by water X, NO XWith the effect of flue dust, the water in the purifying box is realized exchange heat by the water in heat pipe and the water jacket simultaneously.But this device is not suitable for using at tubular heater, the flue-gas temperature that the tubular heater convection section comes out is at 330~340 ℃, such high-temperature flue gas passes through water, water will be vaporized, simultaneously tubular heater finally will be realized is heat exchange between flue gas and the combustion air, and the function of this device is the heat exchange between the cigarette G﹠W.Chinese patent CN2275200Y discloses a kind of " boiler fume desulfurizing and dedusting air preheater ", comprise Heat Room, impulse chamber, cesspool, spray chamber and dash chamber, the impulse chamber is positioned at the Heat Room bottom, cesspool is positioned at bottom, impulse chamber, spray chamber is positioned at impulse chamber and cesspool one side, boiler dust-laden sulfur contained high temoperature flue gas elder generation after the air heat exchange, realizes dedusting and desulfurization through impulse, spray and dash through Heat Room again.The structure of this device is that air preheater and flue gas desulfurization purifier are arranged in proper order, directly enter impulse chamber waste heat can be not fully utilized after the Heat Room heat exchange if be used on the tubular heater flue gas, and acid dew piont corrosion easily takes place Heat Room equipment.
Existing waste heat of flue gas of heating furnace removal process synchronized desulfuring and denitrifying purification techniques perhaps is prone to acid dew piont corrosion and waste heat recovery efficient problem on the low side owing to exist and can't use at tubular heater when using.Make the application of this technology on the Petrochemical Enterprises tubular heater be restricted, restricted carrying out of enterprise's " energy-saving and emission-reduction " work, require further improvement solution.
Goal of the invention
The purpose of this invention is to provide a kind of method for petroleum refining, the purification of petrochemical industry tubular heater flue gas waste heat recovery process synchronized desulfuring and denitrifying.Be used for solving prior art and acid dew piont corrosion and waste heat recovery efficient problem on the low side can't when tubular heater is used or used, occur.
Technical scheme
For addressing the above problem, the technical solution used in the present invention is: a kind of flue gas waste heat recovery desulfurization denitration method, and this method is made up of following steps:
1) temperature is 300~360 ℃, is preferably 330~340 ℃ and contains SO X, NO XFlue gas enters the air heat exchange of preheater and 60~70 ℃, and the air themperature of heat exchange reaches 200~210 ℃, and to send into combustion system combustion-supporting, and the flue gas of heating furnace that cools to 180~190 ℃ enters into step 2);
2) be preferably 180~190 ℃ of flue gases from 150~220 ℃ of step 1) and enter the absorption tower, contact with absorption liquid, absorbed SO X, NO XAbsorption liquid flow into the bottom, absorption tower, absorption liquid recycles, absorption liquid is passed to the heat pipe low-temperature end with heat, the flue gas that purifies 80~90 ℃ of backs enters atmosphere.Receive liquid heat is passed to the heat pipe temperature end, keep absorption liquid to SO in the flue gas XRemoval efficiency 〉=70%.
3) air from atmosphere enters air preheater and the heat exchange of heat pipe temperature end, and temperature is upgraded to 60~70 ℃ and enters step 1).
Utilize and add new absorption liquid and discharge SO X, NO XThe method of absorption liquid is kept absorption liquid to SO in the flue gas XRemoval efficiency 〉=70%.
Described flue gas is for containing SO X, NO XTemperature is 300~360 ℃ flue gas, comprising: flue gas of heating furnace, boiler smoke, catalytic cracking regenerator flue gas, industrial furnace flue gas, coke oven flue gas etc.
Described 180~190 ℃ of flue gases enter absorption tower and absorption liquid counter current contacting.
Described 180~190 ℃ of flue gases enter the absorption tower and contact with the absorption liquid bubbling.
Described heat pipe is operating temperature at 50~250 ℃ normal temperature heat pipe.
A kind of flue gas waste heat recovery desulfuring and denitrifying apparatus comprises absorption tower, high-temperature preheater, air preheater and heat pipe, is characterised in that: the low-temperature end of heat pipe is arranged on inside, absorption tower, and the temperature end heat exchange is arranged in the air preheater.
The low-temperature end of described heat pipe is arranged on the bottom, absorption tower.
Has corrosive SO in the flue gas X, NO XBecome sulfate and nitrate with absorption liquid generation chemical reaction, flue dust sinks to desulfurizing tower bottom, and absorption liquid is passed to air in the air preheater to heat by the high-performance heat transfer components heat pipe simultaneously.
Beneficial effect of the present invention
Compared with prior art, a kind of flue gas waste heat recovery desulfurization denitration method has following advantage:
(1) after high-temperature flue gas earlier reduces uniform temperature with the air heat exchange in high-temperature preheater, enters the absorption tower again, SO in the high-temperature flue gas X, NO XWith NH 3H 2The endothermic process that the exothermic process that O generation chemical reaction need be lowered the temperature and combustion air need heat up effectively combines, make the complementation that is optimized of the heat energy utilization of two separate units, thereby make this technology can be when the Petrochemical Enterprises tubular heater is used, heat exchange process obtains simplifying, and waste heat recovery efficient is improved;
(2) be in the SO that contains on the acid dew-point temperature X, NO XFlue gas enter the absorption tower namely with absorption liquid NH 3H 2Chemical reaction takes place in O, generates sulfate and nitrate, has reduced possibility and discharge of harmful gases that acid dew piont corrosion takes place;
(3) absorption liquid absorbs SO in the high-temperature flue gas on the absorption tower X, NO XIn the time of with flue dust, the exchange of realization and high-temperature flue gas heat synchronously, absorption liquid is to remove SO in the high-temperature flue gas X, NO XWith the medicament of flue dust, be again the hot media of realizing high-temperature flue gas and air heat exchange, thereby the device structure that flue gas waste heat recovery and desulphurization denitration are purified obtain simplifying.
The method that waste heat of flue gas of heating furnace removal process synchronized desulfuring and denitrifying of the present invention purifies is owing to adopt heat exchange process and the gas cleaning step of optimizing, make this technology can be when the Petrochemical Enterprises tubular heater is used, waste heat recovery efficient is further enhanced, the possibility of equipment generation acid dew piont corrosion is further reduced, floor space is few, the device one-time investment is little, has significantly improved the technical merit that existing waste heat of flue gas of heating furnace reclaims and desulphurization denitration purifies.
Description of drawings
The present invention is further detailed explanation below in conjunction with the drawings and specific embodiments.
Fig. 1 is a kind of flue gas waste heat recovery desulfurization denitration method of the present invention schematic flow sheet.
Wherein: 1-goes out the air preheater air line, the import of 2-high-temperature preheater heat exchange coil, 3-high-temperature preheater, 4-high-temperature preheater gas approach, the outlet of 5-high-temperature preheater heat exchange coil, 6-high-temperature preheater heat exchange coil, 7-high-temperature preheater exhanst gas outlet, the 8-absorption liquid goes out the circulating pump pipeline, the import of 9-adsorption tower smoke, ammonia mouth, 11-circulating pump are annotated in the 10-absorption tower, the 12-absorption liquid advances the circulating pump pipeline, the 13-absorption liquid, 14-absorption tower floss hole, 15-absorption tower, the import of 16-air preheater, the 17-heat pipe, 18-air preheater, the outlet of 19-air preheater, the 20-spray head, the outlet of 21-adsorption tower smoke.
The specific embodiment
Referring to Fig. 1, be the method that the present invention is applied to a kind of flue gas waste heat recovery process synchronized desulfuring and denitrifying of tubular heater, be provided with high-temperature preheater, absorption tower, air preheater.
Flue gas is flue gas of heating furnace, and flue gas is come temperature between 330~340 ℃ from the heating furnace convection section, SO XContent is sometimes up to several thousand ppm, if flue gas directly enters the absorption tower this moment, absorption liquid can because flue-gas temperature too up to less than due assimilation effect, low temperature is conducive to absorption liquid to SO XAbsorption.And high temperature can cause the evaporation of absorption liquid, influences normal waste heat recovery and gas cleaning operation.Therefore need earlier 330~340 ℃ high-temperature flue gas in high-temperature preheater with 60~70 ℃ the air heat exchange of coming from air preheater, enter absorption tower heat exchange and desulfurization again after flue-gas temperature is reduced to 180~190 ℃.The high-temperature flue gas temperature difference of 60~70 ℃ air and 330~340 ℃ is bigger, and both heat exchange effects are better.High-temperature preheater is mature technology, can adopt types such as tubulation, plate-fin or heat pipe.
Temperature is reduced to 180~190 ℃ sulfur-containing smoke gas and is entered the absorption tower in the described method, fully contacts SO wherein with absorption liquid adverse current under the spray nozzle spray X, NO X, flue dust and heat fall into the bottom, absorption tower after being absorbed by liquid absorption, and has corrosive SO in the flue gas XWith absorption liquid NH 3H 2Chemical reaction takes place and becomes sulfate in O:
SO 2+ H 2O=H 2SO 3(sulfurous acid)
NH 3+ H 2O=NH 4OH (ammoniacal liquor)
2NH 4OH+H 2SO 3=(NH 4) 2SO 3(ammonium sulfite)+2H 2O
Has corrosive SO in the flue gas XOnly be lower than acid dew-point temperature in flue-gas temperature, in the time of generally<140 ℃ just acid dew piont corrosion can take place, temperature is namely to generate sulfate with absorption liquid generation chemical reaction after 180~190 ℃ sulfur-containing smoke gas enters the absorption tower, has reduced the possibility of sulfur-containing smoke gas generation acid dew piont corrosion.Has corrosive NO in the flue gas XWith absorption liquid NH 3H 2Chemical reaction takes place and becomes nitrate in O:
2NO+O 2=2NO 2
2NO 2+H 2O=HNO 3+HNO 2
NH 3+HNO 3=HN 4NO 3+H 2O
NH 3+HNO 2=HN 4NO 2+H 2O
Flue dust is absorbed by liquid absorption the back and sinks to the bottom, absorption tower by gravity, simultaneously absorption liquid is passed to air in the air preheater to heat by the high-performance heat transfer components heat pipe, heat pipe is a kind of heat transfer element with high heat conductivility, it is by transmitting heat in the phase transformation of Totally enclosed vacuum liquid in pipe, the heat conduction of velocity is very fast, can make the temperature of absorption liquid maintain the suitable SO in the flue gas that absorbs all the time in time the air in the heat transferred air preheater of bottom, absorption tower absorption liquid X, NO XScope in, thereby guarantee the assimilation effect of realizing ideal.The absorption liquid of bottom, absorption tower enters spray head by circulating pump, nebulizes from the spray head spray down, meets with flue gas adverse current, and full contact absorbs fully SO in the flue gas X, NO X, after flue dust and heat be absorbed by liquid absorption, become clean free of contamination temperature at 80~90 ℃ low wet, export into from the absorption tower and enter atmosphere behind the chimney.
20~30 ℃ of air of coming from atmosphere in the described method are in air preheater and heat pipe heat exchanging, temperature is upgraded to 60~70 ℃, enter the import of high-temperature preheater heat exchange coil from air preheater outlet (19) through air line, in heat exchange coil with 330~340 ℃ of high-temperature flue gas heat exchange of coming from the heating furnace convection section after temperature be upgraded to 200~210 ℃, it is combustion-supporting to send into the heating furnace combustion system through the outlet of high-temperature preheater heat exchange coil.
Along with the increase of sulfate, nitrate and dust concentration in the absorption liquid of absorption tower, absorption liquid absorbs SO in the flue gas X, NO XCan reduce with the ability of flue dust, therefore should regularly emit a part of absorption liquid from the floss hole of bottom, absorption tower, the notes ammonia mouth from the absorption tower sidepiece injects fresh ammoniacal liquor simultaneously, to keep the stronger absorbability of absorption liquid.The absorption liquid aerating oxygen of emitting, sulfate wherein generates sulfate of ammoniac, does the concentrated fertilizer of basic soil, twice laid, very environmental protection.
(NH 4) 2SO 3+1/2O 2=(NH 4) 2SO 4
Below in conjunction with description of drawings operating process of the present invention.A) temperature is that 20~30 ℃ air enters air preheater from atmosphere from the air preheater import, and entering high-temperature preheater through air line, to send into the heating furnace combustion system combustion-supporting.B) inject the ammoniacal liquor absorption liquid of certain liquid level from absorption tower notes ammonia mouth toward the absorption tower, liquid level is minimum will not to have superheater tube, open the absorption liquid circulating pump, absorption liquid is rained from the spray head spray form vaporific absorption liquid in the absorption tower, vaporific absorption liquid rain falls into the bottom, absorption tower and forms circulation through the absorption liquid circulating pump in tower.C) draw 330~340 ℃ high-temperature flue gas and enter high-temperature preheater, flue gas and air heat exchange in high-temperature preheater, normal circulation along with flue gas and air, 20~30 ℃ air goes out the air preheater temperature and is upgraded to 60~70 ℃ and enters high-temperature preheater, flue gas is reduced to 180~190 ℃ with 60~70 ℃ air heat exchange temperature in high-temperature preheater, air goes out the high temperature preheating actuator temperature and is upgraded to 200~210 ℃.D) contain SO X, NO XEnter the absorption tower with 200~210 ℃ of flue gas self-absorption tower entrances of flue dust, fully contact SO in the flue gas with vaporific absorption liquid adverse current under spray head spray X, NO X, after flue dust and heat be absorbed by liquid absorption, become clean free of contamination temperature at 80~90 ℃ low wet, export into from the absorption tower and enter atmosphere behind the chimney.E) through certain hour, the time interval is with SO in the flue gas X, NO XWith the content of flue dust and different, sulfate, nitrate and dust concentration constantly increase in the absorption liquid, the absorbability of absorption liquid can reduce, must emit a part of absorption liquid from the floss hole of bottom, absorption tower, notes ammonia mouth from the absorption tower sidepiece injects fresh ammoniacal liquor simultaneously, to keep the stronger absorbability of absorption liquid.
The aforesaid operations process can not be put upside down, if high-temperature preheater heat exchange coil bubbling air in advance not, 330~340 ℃ high-temperature flue gas will directly not enter the absorption tower through cooling and contact with absorption liquid, causes absorption liquid to seethe with excitement and vaporizes, and influences normal operating and finishes.

Claims (10)

1. flue gas waste heat recovery desulfurization denitration method is characterized in that: be made up of following steps:
1) temperature is 300~360 ℃ and contains SO X, NO XFlue gas enters the air heat exchange of preheater and 60~70 ℃, and air themperature reaches 200~210 ℃ to send into combustion system combustion-supporting after the heat exchange, and the flue gas that cools to 150~220 ℃ enters into step 2);
2) enter the absorption tower from 150~220 ℃ of flue gases of step 1) and contact with absorption liquid, absorbed SO X, NO XAbsorption liquid flows into the bottom, absorption tower, and absorption liquid recycles, and absorption liquid is passed to the heat pipe low-temperature end with heat, and 80~90 ℃ of flue gases after the purification enter atmosphere, keep absorption liquid to SO in the flue gas XRemoval efficiency 〉=70%;
3) air from atmosphere enters air preheater and the heat exchange of heat pipe temperature end, and temperature is upgraded to 60~70 ℃ and enters step 1).
2. according to the described a kind of flue gas waste heat recovery desulfurization denitration method of claim 1, it is characterized in that: described temperature is 330~340 ℃ and contains SO X, NO XFlue gas enters the air heat exchange of preheater and 60~70 ℃, and the air themperature of heat exchange reaches 200~210 ℃, and to send into combustion system combustion-supporting, and the flue gas that cools to 180~190 ℃ enters into step 2).
3. according to the described a kind of flue gas waste heat recovery desulfurization denitration method of claim 1, it is characterized in that: described flue gas is for containing SO X, NO XTemperature is 300~360 ℃ flue gas, contains a kind of in flue gas of heating furnace, boiler smoke, regeneration fume from catalytic cracking, industrial furnace flue gas, the coke oven flue gas at least.
4. according to the described a kind of flue gas waste heat recovery desulfurization denitration method of claim 1, it is characterized in that: described 150~220 ℃ of flue gases enter absorption tower and absorption liquid counter current contacting.
5. according to the described a kind of flue gas waste heat recovery desulfurization denitration method of claim 1, it is characterized in that: described 150~220 ℃ of flue gases enter the absorption tower and contact with the absorption liquid bubbling.
6. according to the described a kind of flue gas waste heat recovery desulfurization denitration method of claim 1, it is characterized in that: described heat pipe is operating temperature at 50~250 ℃ heat pipe.
7. according to the described a kind of flue gas waste heat recovery desulfurization denitration method of claim 1, it is characterized in that: described absorption liquid is to SO in the flue gas XRemoval efficiency 〉=70%.
8. flue gas waste heat recovery desulfuring and denitrifying apparatus, by comprising that absorption tower, high-temperature preheater, air preheater and heat pipe form, be characterised in that: the low-temperature end of heat pipe is arranged on inside, absorption tower, and the temperature end heat exchange is arranged in the air preheater.
9. according to the described a kind of flue gas waste heat recovery desulfuring and denitrifying apparatus of claim 8, it is characterized in that: the low-temperature end of described heat pipe is arranged on the bottom, absorption tower.
10. according to the described a kind of flue gas waste heat recovery desulfuring and denitrifying apparatus of claim 8, it is characterized in that: the temperature end of described heat pipe is arranged on the bottom, absorption tower.
CN2012100500751A 2012-03-01 2012-03-01 Flue gas afterheat-recycling, desulfurizing and denitrifying method and device CN103292604A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109200963A (en) * 2018-09-05 2019-01-15 辽宁盛达环保科技发展有限公司 Efficient coupling, Poly-generation, the activating coal gangue technique of low nitrogen

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CN101062461A (en) * 2007-04-27 2007-10-31 南京师范大学 Method and system for combinablenably removing SO2, NOx and Hg in coal smoke gas by using recombustion of biomass
CN101279186A (en) * 2008-05-23 2008-10-08 清华大学 Flue gas dry-type method for simultaneously desulfurizing and denitrating
CN101298021A (en) * 2008-01-22 2008-11-05 王敏 Gas-liquid contact type non-phase-change middle medium heat exchange wet-type desulfuration method and apparatus

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1301584A (en) * 1999-12-30 2001-07-04 赵善茂 Complex utilization method for boiler fume
WO2006030398A1 (en) * 2004-09-16 2006-03-23 Elsam Engineering A/S Method of operating a flue gas cleaning plant
CN101062461A (en) * 2007-04-27 2007-10-31 南京师范大学 Method and system for combinablenably removing SO2, NOx and Hg in coal smoke gas by using recombustion of biomass
CN101298021A (en) * 2008-01-22 2008-11-05 王敏 Gas-liquid contact type non-phase-change middle medium heat exchange wet-type desulfuration method and apparatus
CN101279186A (en) * 2008-05-23 2008-10-08 清华大学 Flue gas dry-type method for simultaneously desulfurizing and denitrating

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109200963A (en) * 2018-09-05 2019-01-15 辽宁盛达环保科技发展有限公司 Efficient coupling, Poly-generation, the activating coal gangue technique of low nitrogen

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Application publication date: 20130911