CN101695627A - Dry-method fume gas purification method and device for synchronous desulfurization and denitrification - Google Patents

Dry-method fume gas purification method and device for synchronous desulfurization and denitrification Download PDF

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CN101695627A
CN101695627A CN200910112733A CN200910112733A CN101695627A CN 101695627 A CN101695627 A CN 101695627A CN 200910112733 A CN200910112733 A CN 200910112733A CN 200910112733 A CN200910112733 A CN 200910112733A CN 101695627 A CN101695627 A CN 101695627A
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absorbent
absorption tower
fluidized bed
fume
dry
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CN200910112733A
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CN101695627B (en
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王建春
张志文
张原�
林驰前
郑进朗
詹威全
余华龙
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福建龙净脱硫脱硝工程有限公司
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Abstract

The invention relates to fume purification and provides dry-method fume purification method and device for synchronous desulfurization and denitrification. The purification device is provided with an inlet flue, an absorption tower, a dust collector, a material circulating air chute, an absorbent cabin, a water box, a water pump, an atomization spray gun and an outlet flue. In the invention, an additive water solution is stored in a process water box; a primary fume enters the absorption tower through the inlet flue, mixes with an absorbent added form the absorbent cabin and cycled materials returned from the material circulating air chute, and then performs cooling and moistening reaction with the additive water solution pumped by the high-pressure pump from the water box to the atomization spray gun and sprayed by the atomization spray gun to the absorption tower; the outlet fume of the absorption tower enters the dust collector, incompletely reacted materials in the fume are collected, and the major part of the fume enters a circulating fluidize bed absorption tower with the absorbent added in the absorbent cabin through the material circulating air chute to continue the reaction; circulation continues in the same way; and the fume purification is then achieved when the cleaned fume is exhausted from a chimney from the dust collector through the outlet flue.

Description

The dry-method fume gas purification method and the device of while desulphurization denitration

Technical field

The present invention relates to a kind of gas cleaning, especially relate to a kind of dry-method fume gas purification method and device of desulphurization denitration simultaneously realized.

Background technology

The SO that coal burning is discharged 2And NO xIt is the main cause that causes atmosphere pollution.Generally adopt FGD (flue gas desulfurization) to carry out desulphurization denitration at present with the method that SCR (selective-catalytic-reduction denitrified) combines, the method that this classification is handled is higher to pollutant removing efficient, but investment is also higher with operating cost, and complex process, equipment is various, occupation of land is very big.

Zhang Ze etc. disclose a kind of dry method flue gas cleaning technology and system thereof of while desulphurization denitration in the patent No. is the Chinese invention patent of ZL 03125332.6.This process using hydrogen peroxide or methyl alcohol make the nitric oxide in the flue gas be converted into nitrogen dioxide as additive; Adopt calcium base particle as the desulfurizing agent desulfurization again; Adopt ammoniacal liquor or urea to absorb nitrogen dioxide at last as denitrfying agent.Adopt this technology can obtain satisfied desulfurization, denitration efficiency, water consumption is less.But this technological process is still comparatively complicated, and each system level such as desulfurization, denitration is handled, and operation is loaded down with trivial details.Particularly whole system is provided with 3 cover cleaners, adds additive injection device, circulating fluidization dry flue gas desulphurization system and dry method denitrating system etc., and the integral device investment is bigger, and practical application is restricted.

Zhao Yi etc. disclose a kind of flue gas desulfuration and denitrification purification method in the patent No. is the Chinese invention patent of ZL200310103954.7.It is to spray into a kind of highly active absorbent to reach the purpose of desulphurization denitration simultaneously in circulating fluid bed reactor.This highly active absorbent is flyash, calcium hydroxide and the additive of certain proportioning, and wherein additive is one or more in potassium permanganate, calcium hypochlorite, ammonium persulfate and the Peracetic acid.This method can reach desulfuration efficiency and the 60% above denitration efficiency more than 90% simultaneously, has simple, the stable and non-wastewater discharge of equipment and does not produce advantage such as secondary pollution.But the preparation method of the highly active absorbent that this method adopted is loaded down with trivial details, is difficult to solve raw material transportation, storage, preparation and the use problem of a large amount of absorbents in the industrial applications process; And the additive instability lost efficacy easily at higher temperature with after placing the long period, had reduced its practical value, was difficult to really realize industrial applications.

Summary of the invention

The objective of the invention is to defective, a kind of dry-method fume gas purification method and device of desulphurization denitration simultaneously realized is provided at the said method existence.

The dry method smoke eliminator of while desulphurization denitration of the present invention is provided with gas approach, recirculating fluidized bed reaction absorption tower, deduster, material circulating air skewed slot, absorbent storehouse, sulfur removal technology water tank, high-pressure hydraulic pump, atomizing lance, exhaust pass, associated supports and connecting pipe; The gas approach on recirculating fluidized bed reaction absorption tower is by the external flue gas that needs purification of gas approach, the absorbent import of being located at recirculating fluidized bed reaction bottom, absorption tower connects the absorbent storehouse, atomizing lance is located at the fresh water (FW) import on recirculating fluidized bed reaction absorption tower, the atomizing lance water inlet connects high-pressure hydraulic pump through water pipe, the high-pressure hydraulic pump water inlet connects the sulfur removal technology water tank, the exhanst gas outlet of being located at recirculating fluidized bed reaction top, absorption tower connects deduster, the material outlet of deduster connects the material inlet of material circulating air skewed slot, the material outlet of material circulating air skewed slot is connected with the recycle stock import of returning on recirculating fluidized bed reaction absorption tower, the cleaning flue gases outlet of deduster is discharged through exhaust pass and by chimney, and the accessory substance that deduster produces effluxes by material outlet and fully utilizes.

The dry-method fume gas purification method of while desulphurization denitration of the present invention may further comprise the steps:

1) the additive aqueous solution is stored in the technology water tank;

2) will need the former flue gas that purifies to enter recirculating fluidized bed reaction absorption tower by gas approach, after recycle stock that absorbent that adds from the absorbent storehouse and material circulating air skewed slot return mixes, and be evacuated to the additive aqueous solution that atomizing lance sprays into from the technology water tank through high-pressure hydraulic pump and carry out decreasing temperature and increasing humidity and react;

3) outlet flue gas in recirculating fluidized bed reaction absorption tower enters deduster, unreacted is after the material ash is captured completely in the flue gas, most of absorbent that adds with the absorbent storehouse by material circulating air skewed slot enters recirculating fluidized bed reaction absorption tower and continues to participate in reaction, so circulation;

4) the cleaning flue gases Self-duster is discharged toward chimney through exhaust pass, finally finishes the purification of flue gas.

In step 1), described additive can adopt potassium permanganate (KMnO 4), calcium hypochlorite (Ca (ClO) 2) and sodium chlorite (NaClO 2) etc. at least a in the strong oxidizing property additive.

In step 2) in, described absorbent can adopt calcium hydroxide (Ca (OH) 2) or quick lime (CaO), press mass ratio, the consumption of absorbent can be controlled in Ca: (S+0.5N) be 1: (1.1~1.5); The consumption of fresh water (FW) can be controlled in and makes clean flue gas cool-down to 70~90 ℃ institute's water consumption; The consumption of described additive can be controlled to be 1%~5% of absorbent.

Spray into the strong oxidizing property additive fraction that is dissolved in the water in the tower and directly contact, by the strong oxidation reaction generation NO soluble in water of additive with NO in the flue gas with the solution form 2Most of being attached to after the water evaporates on the high density absorbent material particles, original position is uniformly mixed to form highly active " rich oxygen type " absorbent is by the oxidation and the catalytic action of additive, in conjunction with O in the flue gas 2Generate NO soluble in water with the NO reaction 2Simultaneously, part SO in the flue gas 2Change into SO with the additive reaction of strong oxidizing property 3SO in the final flue gas 3/ SO 2And NO 2With removing after the calcium-base absorbing agent reaction, finish desulfurization and denitrification reaction simultaneously.The fresh water (FW) consumption is decided according to former flue-gas temperature and clean flue-gas temperature, and additive amount is decided according to the additive types of absorbent consumption and selection.Described former flue gas is the unprocessed SO that contains 2And NO xDeng the recirculating fluidized bed reaction absorption tower inlet flue gas of pollutant, clean flue gas is the recirculating fluidized bed reaction absorption tower outlet flue gas after desulphurization denitration is handled.Described " rich oxygen type " absorbent is the calcium-base absorbing agent that contains the strong oxidizing property additive.The desulfurization and denitrification reaction process duration is about 6s in the recirculating fluidized bed reaction absorption tower.

In step 3), described circulation can reach hundreds of times, effluxes as accessory substance on a small quantity to fully utilize.Described recycle stock main component is unreacted absorbent Ca (OH) completely 2The described accessory substance main component that effluxes is CaSO 31/2H 2O, CaSO 4, Ca (NO 3) 2And Ca (NO 2) 2, also comprise a small amount of CaCO 3, CaCl 2And unreacted CaO, Ca (OH) completely 2Deng, whole meta-alkalescence, very stable under natural environment, do not have secondary pollution, but integrated application is in mine landfill, brickmaking, purposes such as pave the way.

The dry cleaning device of flue gas and desulfurizing and denitrifying of realizing of the present invention is provided with gas approach, recirculating fluidized bed reaction absorption tower, deduster, material circulating air skewed slot, absorbent storehouse, technology water tank, high-pressure hydraulic pump, atomizing lance, exhaust pass, associated supports and connecting pipe.The former flue gas that needs to purify is introduced recirculating fluidized bed reaction absorption tower by gas approach, the absorbent import of recirculating fluidized bed reaction bottom, absorption tower connects the absorbent storehouse, the fresh water (FW) porch dress atomizing lance on recirculating fluidized bed reaction absorption tower, atomizing lance connects the technology water tank through high-pressure hydraulic pump, the exhanst gas outlet on recirculating fluidized bed reaction top, absorption tower connects deduster, the material outlet of deduster connects the material inlet of material circulating air skewed slot, the material outlet of material circulating air skewed slot is connected with the recycle stock import of returning on recirculating fluidized bed reaction absorption tower, the cleaning flue gases outlet of deduster is discharged toward chimney through exhaust pass, and the accessory substance that deduster produces effluxes by material outlet and fully utilizes.

The additive aqueous solution is being stored in the technology water tank, and the additive aqueous solution of the ratio preparation variable concentrations of additive in the adding technology water tank and fresh water (FW) can be according to NO in the flue gas xConcentration adjustment.

The present invention with recirculating fluidized bed as the reaction absorption tower, the solubility absorbent additive of strong oxidizing property is dissolved in the fresh water (FW), high-pressure hydraulic pump by the fresh water (FW) system is evacuated to atomizing lance and follows decreasing temperature and increasing humidity water to spray in the absorption tower, utilize the oxidation and the catalytic action of additive, at short notice with flue gas in NO reaction change into NO soluble in water 2, then with SO 2Be added into the calcium-base absorbing agent absorbing and removing in the absorption tower together, reach the purpose of desulphurization denitration simultaneously.The solubility absorbent additive of described strong oxidizing property is potassium permanganate KMnO 4, calcium hypochlorite Ca (ClO) 2With sodium chlorite NaClO 2In one or more raw material combination.Described calcium-base absorbing agent is calcium hydroxide Ca (OH) 2Or quick lime CaO.

The present invention adopts recirculating fluidized bed as the absorption tower, and the strong oxidizing property soluble additive is sprayed into the absorption tower by the fresh water (FW) system.Reaction mechanism in recirculating fluidized bed reaction absorption tower is that material is in recirculating fluidized bed; the gas-solid two-phase produces fierce turbulence and mixes; fully contact; landing speed between gas-solid is up to tens of times of individual particle landing speed; greatly strengthened the heat and mass transport between gas-solid, formed the bed of material with huge specific area.When spraying into atomizing when containing the additive aqueous solution of strong oxidizing property, SO in the flue gas 2Deng sour gas and absorbent Ca (OH) 2Deng reaction be converted into the reaction of ionic type that can finish moment; Reduce flue-gas temperature simultaneously to more than the dew point about 15 ℃, the water that assurance sprays into can evaporate fully, most of strong oxidizing property additive is retained in the absorbent surface original position to high degree of dispersion and forms high activity " rich oxygen type " absorbent after the water evaporation, strong oxidation and catalytic action by additive utilize O in the flue gas 2NO is converted into NO 2, finish denitrification process with calcium-base absorbing agent generation neutralization reaction again.In the desulphurization denitration process, when Ca/ (S+0.5N) is 1.2, the fresh water (FW) consumption makes clean flue gas cool-down to 75 ℃, when additive amount is absorbent 3%, can obtain 93% desulfuration efficiency and 78% denitration efficiency simultaneously.

Compared with prior art, the present invention has following outstanding advantage:

1) use a kind of absorbent in an absorption tower, to finish the desulphurization denitration process simultaneously, each that greatly simplified to satisfying that desulfurization and denitration be provided with respectively independently removes system and technological process, can not only on the industrialization smoke eliminator, reach satisfied in denitrification efficiency, and have that technological process is simple, advantage such as operation maintenance is convenient, floor space is little, water consumption is few, investment and operating cost are lower.

2) by the fresh water (FW) system strong oxidizing property additive is sprayed in the reaction absorption tower, high activity " rich oxygen type " absorbent of original position synthetic additive high degree of dispersion has been simplified the absorbent preparation process, has greatly improved the result of use of additive.

3) denitrification efficiency height.After testing, desulfuration efficiency is more than 90%, to reach as high as 99%; Denitration efficiency is more than 68%, to reach as high as 92%; The complete qualified discharge of flue gas.

4) whole process does not produce secondary pollution.

5) have universality, Technological Economy is excellent, is applicable to the smoke gas treatment of coal-burning power plant and various Industrial Stoves, and market prospects are wide.

Description of drawings

Fig. 1 is that the structure of the dry method smoke eliminator of while desulphurization denitration of the present invention is formed schematic diagram.In Fig. 1, each mark is defined as: 1 gas approach, 2 recirculating fluidized beds reaction absorption tower, 3 dedusters, 4 material circulating air skewed slots, 5 absorbent storehouses, 6 sulfur removal technology water tanks, 7 high-pressure hydraulic pumps, 8 atomizing lances, 9 exhaust pass.

The specific embodiment

Fig. 1 provides the dry method smoke eliminator embodiment of while desulphurization denitration of the present invention, and this device is provided with gas approach 1, recirculating fluidized bed reaction absorption tower 2, deduster 3, material circulating air skewed slot 4, absorbent storehouse 5, sulfur removal technology water tank 6, high-pressure hydraulic pump 7, atomizing lance 8, exhaust pass 9, associated supports and connecting pipe; The gas approach on recirculating fluidized bed reaction absorption tower 2 is by the gas approach 1 external flue gas that needs purification, the absorbent import 21 of being located at recirculating fluidized bed reaction 2 bottoms, absorption tower connects absorbent storehouse 5, atomizing lance 8 is located at the fresh water (FW) import on recirculating fluidized bed reaction absorption tower 2, atomizing lance 8 water inlets connect high-pressure hydraulic pump 7 through water pipe, high-pressure hydraulic pump 7 water inlets connect sulfur removal technology water tank 6, the exhanst gas outlet 22 of being located at recirculating fluidized bed reaction 2 tops, absorption tower connects deduster 3, the material outlet 31 of deduster 3 connects the material inlet of material circulating air skewed slot 4, the material outlet of material circulating air skewed slot 4 is connected with the recycle stock import of returning on recirculating fluidized bed reaction absorption tower 2, the cleaning flue gases outlet 32 of deduster 3 is discharged through exhaust pass 9 and by chimney, and the accessory substance that deduster 3 produces effluxes by material outlet and fully utilizes.

Below provide the embodiment that the dry method smoke eliminator that adopts the described while desulphurization denitration of Fig. 1 carries out gas cleaning.

Embodiment 1

Certain power plant uses the dry method smoke eliminator of while desulphurization denitration of the present invention to carry out gas cleaning and handles, and generating set capacity is 200MW, and exhaust gas volumn is 1,440,000m 3/ h, former flue gas SO 2Concentration is 3100mg/m 3, former flue gas NO xConcentration is 1100mg/m 3, former smoke inlet temperature is 140 ℃, uses Ca (OH) 2As absorbent, Ca/ (S+0.5N) is 1.2, and promptly the absorbent use amount is 10.88t/h, selects KMnO 4As the absorbent additive.

1. dispose the certain density additive aqueous solution and be stored in the technology water tank, the additive addition is absorbent 1%, i.e. KMnO 4Use amount is 0.11t/h.

2. the former flue gas that needs to purify enters recirculating fluidized bed reaction absorption tower 2 by gas approach 1, after following recycle stock that absorbent that absorbent storehouse 5 adds and material circulating air skewed slot 4 return and mixing, and be evacuated to the additive KMnO that atomizing lance 8 sprays into through high-pressure hydraulic pump 7 from technology water tank 6 4The aqueous solution carries out decreasing temperature and increasing humidity and oxidation absorption reaction, sprays into aqueous solution total amount and guarantees that exit gas temperature is about 72 ℃.Spray into the strong oxidizing property additive KMnO that is dissolved in the water in the tower 4Fraction is directly to contact with NO in the flue gas in solution, by additive KMnO 4Strong oxidation reaction generate NO soluble in water 2Most of KMnO 4After water evaporates,, be uniformly mixed to form highly active " rich oxygen type " absorbent, pass through KMnO with high density absorbent material particles original position attached to above the absorbent 4Oxidation and catalytic action, in conjunction with O in the flue gas 2Generate NO soluble in water with the NO reaction 2Simultaneously, part SO in the flue gas 2With pass through KMnO 4Oxidation and catalytic action in conjunction with O in the flue gas 2Reaction changes into SO 3SO in the final flue gas 3/ SO 2And NO 2With absorbent Ca (OH) 2Remove after the reaction, finish desulfurization and denitrification reaction simultaneously.Whole desulfurization and denitrification reaction process duration in recirculating fluidized bed reaction absorption tower is about 6s.

3. outlet flue gas in absorption tower enters deduster 3, and unreacted is after the material ash is captured completely in the flue gas, and most of unreacted is absorbent Ca (OH) completely 2The absorbent that adds with absorbent storehouse 5 by material circulating air skewed slot 4 enters the 2 continuation participation reactions of recirculating fluidized bed reaction absorption tower, and so circulation can reach hundreds of times, effluxes as accessory substance on a small quantity to fully utilize.

4. cleaning flue gases Self-duster 3 is discharged toward chimney through exhaust pass 9, finally finishes the purification of flue gas.

After testing, export clean flue gas SO 2Concentration is 278mg/m 3, desulfuration efficiency reaches 91%; NO xConcentration is 352mg/m 3, denitration efficiency reaches 68%.It is most of with CaSO to efflux the accessory substance ash 31/2H 2O, CaSO 41/2H 2O, Ca (NO 2) 2And Ca (NO 3) 2Form exists, and comprises a small amount of CaCO 3, CaCl 2, MnO 2, and unreacted CaO, Ca (OH) completely 2Deng, there is not secondary pollution in whole meta-alkalescence, but integrated application is in mine landfill, brickmaking, purposes such as pave the way.

Embodiment 2

Certain power plant uses the dry method smoke eliminator of while desulphurization denitration of the present invention to carry out the gas cleaning processing among the embodiment 1, and service condition is consistent with embodiment 1, and absorbent additive use amount changes to 3% of absorbent consumption, i.e. KMnO 4Use amount is 0.33t/h.After testing, export clean flue gas SO 2Concentration is about 217mg/m 3, desulfuration efficiency reaches 93%; NO xConcentration is about 242mg/m 3, denitration efficiency reaches 78%.

Embodiment 3

Certain power plant uses the dry method smoke eliminator of while desulphurization denitration of the present invention to carry out the gas cleaning processing among the embodiment 1,2, and service condition is consistent with embodiment 1,2, and absorbent additive use amount changes to 5% of absorbent consumption, i.e. KMnO 4Use amount is 0.55t/h.After testing, export clean flue gas SO 2Concentration is 155mg/m 3, desulfuration efficiency reaches 95%; NO xConcentration is 88mg/m 3, denitration efficiency reaches 92%.

Embodiment 4

Certain power plant uses the dry method smoke eliminator of while desulphurization denitration of the present invention to carry out the gas cleaning processing among the embodiment 1, and service condition is consistent with embodiment 1, selects NaClO 2As the absorbent additive, use amount is 2% of absorbent consumption, i.e. NaClO 2Use amount is 0.22t/h.After testing, export clean flue gas SO 2Concentration is 310mg/m 3, desulfuration efficiency reaches 90%; NO xConcentration is 330mg/m 3, denitration efficiency reaches 70%.

Embodiment 5

Certain power plant uses the dry method smoke eliminator of while desulphurization denitration of the present invention to carry out the gas cleaning processing among the embodiment 1, and service condition is consistent with embodiment 1, selects Ca (ClO) 2As the absorbent additive, use amount is 3% of an absorbent consumption, i.e. Ca (ClO) 2Use amount is 0.33t/h.After testing, export clean flue gas SO 2Concentration is 310mg/m 3, desulfuration efficiency reaches 90%; NO xConcentration is 308mg/m 3, denitration efficiency reaches 72%.

Claims (7)

1. the dry method smoke eliminator of while desulphurization denitration is characterized in that being provided with gas approach, recirculating fluidized bed reaction absorption tower, deduster, material circulating air skewed slot, absorbent storehouse, sulfur removal technology water tank, high-pressure hydraulic pump, atomizing lance, exhaust pass, associated supports and connecting pipe; The gas approach on recirculating fluidized bed reaction absorption tower is by the external flue gas that needs purification of gas approach, the absorbent import of being located at recirculating fluidized bed reaction bottom, absorption tower connects the absorbent storehouse, atomizing lance is located at the fresh water (FW) import on recirculating fluidized bed reaction absorption tower, the atomizing lance water inlet connects high-pressure hydraulic pump through water pipe, the high-pressure hydraulic pump water inlet connects the sulfur removal technology water tank, the exhanst gas outlet of being located at recirculating fluidized bed reaction top, absorption tower connects deduster, the material outlet of deduster connects the material inlet of material circulating air skewed slot, the material outlet of material circulating air skewed slot is connected with the recycle stock import of returning on recirculating fluidized bed reaction absorption tower, the cleaning flue gases outlet of deduster is discharged through exhaust pass and by chimney, and the accessory substance that deduster produces effluxes by material outlet and fully utilizes.
2. the dry-method fume gas purification method of desulphurization denitration simultaneously is characterized in that adopting the dry method smoke eliminator of while desulphurization denitration as claimed in claim 1, may further comprise the steps:
1) the additive aqueous solution is stored in the technology water tank;
2) will need the former flue gas that purifies to enter recirculating fluidized bed reaction absorption tower by gas approach, after recycle stock that absorbent that adds from the absorbent storehouse and material circulating air skewed slot return mixes, and be evacuated to the additive aqueous solution that atomizing lance sprays into from the technology water tank through high-pressure hydraulic pump and carry out decreasing temperature and increasing humidity and react;
3) outlet flue gas in recirculating fluidized bed reaction absorption tower enters deduster, unreacted is after the material ash is captured completely in the flue gas, most of absorbent that adds with the absorbent storehouse by material circulating air skewed slot enters recirculating fluidized bed reaction absorption tower and continues to participate in reaction, so circulation;
4) the cleaning flue gases Self-duster is discharged toward chimney through exhaust pass, finally finishes the purification of flue gas.
3. the dry-method fume gas purification method of while desulphurization denitration as claimed in claim 2 is characterized in that in step 1), and described additive adopts at least a in potassium permanganate, calcium hypochlorite, the sodium chlorite.
4. the dry-method fume gas purification method of while desulphurization denitration as claimed in claim 2 is characterized in that in step 2) in, described absorbent adopts calcium hydroxide or quick lime.
5. as the dry-method fume gas purification method of claim 2 or 4 described while desulphurization denitrations, it is characterized in that in step 2) in, press mass ratio, the consumption of described absorbent is controlled at Ca: (S+0.5N) be 1: (1.1~1.5).
6. the dry-method fume gas purification method of while desulphurization denitration as claimed in claim 2 is characterized in that in step 2) in, the consumption of described fresh water (FW) is controlled at and makes clean flue gas cool-down to 70~90 ℃ institute's water consumption.
7. the dry-method fume gas purification method of while desulphurization denitration as claimed in claim 2 is characterized in that in step 2) in, the consumption of described additive is 1%~5% of an absorbent.
CN2009101127333A 2009-10-31 2009-10-31 Dry-method fume gas purification method and device for synchronous desulfurization and denitrification CN101695627B (en)

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CN101856587A (en) * 2010-06-02 2010-10-13 山东大学 Fluidized activated carbon combined desulfurization and denitrification process
CN101940873A (en) * 2010-08-08 2011-01-12 北京北科欧远科技有限公司 Flue gas circulation fluidized bed desulfurizing device provided with corrugated plate
CN102814092A (en) * 2011-06-07 2012-12-12 况保宗 Energy-saving comprehensive desulfurization and denitration dust collector through vortex and particles
CN102961958A (en) * 2012-11-01 2013-03-13 科林环保装备股份有限公司 Integrated system equipment for desulfurization and denitrification of flue gas
CN103386250A (en) * 2013-07-30 2013-11-13 福建龙净脱硫脱硝工程有限公司 Dry desulphurization method
CN105251325A (en) * 2014-07-16 2016-01-20 鞍钢股份有限公司 Sintering flue gas circulating fluidized bed desulphurization and denitrification system and method thereof
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
CN109876625A (en) * 2019-04-15 2019-06-14 昆明理工大学 A kind of dry method simultaneous SO_2 and NO removal method and its system

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CN1247294C (en) * 2003-11-02 2006-03-29 华北电力大学 Method and equipment of desulfurization and denitrogenation for purifying flue gas
CN101306311B (en) * 2008-01-22 2012-07-25 福建龙净脱硫脱硝工程有限公司 Sintered flue gas dry-method removal method and device

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101856587A (en) * 2010-06-02 2010-10-13 山东大学 Fluidized activated carbon combined desulfurization and denitrification process
CN101940873A (en) * 2010-08-08 2011-01-12 北京北科欧远科技有限公司 Flue gas circulation fluidized bed desulfurizing device provided with corrugated plate
CN102814092A (en) * 2011-06-07 2012-12-12 况保宗 Energy-saving comprehensive desulfurization and denitration dust collector through vortex and particles
CN102961958A (en) * 2012-11-01 2013-03-13 科林环保装备股份有限公司 Integrated system equipment for desulfurization and denitrification of flue gas
CN103386250A (en) * 2013-07-30 2013-11-13 福建龙净脱硫脱硝工程有限公司 Dry desulphurization method
CN105251325A (en) * 2014-07-16 2016-01-20 鞍钢股份有限公司 Sintering flue gas circulating fluidized bed desulphurization and denitrification system and method thereof
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
CN109876625A (en) * 2019-04-15 2019-06-14 昆明理工大学 A kind of dry method simultaneous SO_2 and NO removal method and its system

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