CN108579391A - A kind of flue gas purification system utilizing technology based on fume afterheat - Google Patents
A kind of flue gas purification system utilizing technology based on fume afterheat Download PDFInfo
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- CN108579391A CN108579391A CN201810277305.5A CN201810277305A CN108579391A CN 108579391 A CN108579391 A CN 108579391A CN 201810277305 A CN201810277305 A CN 201810277305A CN 108579391 A CN108579391 A CN 108579391A
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- flue gas
- heat exchanger
- water
- absorption tower
- fluidized bed
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/79—Injecting reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8637—Simultaneously removing sulfur oxides and nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/90—Injecting reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Y—GENERAL 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
Abstract
A kind of flue gas purification system utilizing technology based on fume afterheat disclosed in this invention, including recirculating fluidized bed absorption tower and the flue gas cool-down heat exchanger in recirculating fluidized bed absorption tower upstream is set, and the flue gas temperature rise heat exchanger in recirculating fluidized bed absorption tower downstream is set.When the exiting flue gas flow measured value of flue gas cool-down heat exchanger and the ratio of the import flue gas flow design value on recirculating fluidized bed absorption tower are more than 75%, the exiting flue gas on fume afterheat heat cycles fluid bed absorption tower is utilized by flue gas temperature rise heat exchanger, atmosphere hoist height can not only be increased and reduce the groundlevel concentration of pollutant, but also the input gas temperature on recirculating fluidized bed absorption tower can be made to meet the requirement of its normal operation, to solve the problems, such as that the humidification water consumption generated because the input gas temperature on recirculating fluidized bed absorption tower is excessively high is bigger.
Description
Technical field
The present invention relates to filed of flue gas purification, more particularly, to a kind of gas cleaning system utilizing technology based on fume afterheat
System.
Background technology
During thermal power generation, in the flue gas that when fuel combustion releases containing dust, oxysulfide, nitrogen oxides,
The atmosphere pollutions such as dioxin, mercury and mercuric compounds.After not purified flue gas is discharged into air, people's health can be not only given
Harm is brought, but also is likely to form acid rain, photochemical fog.According to the provisions of the relevant regulations issued by the State, newly-built fired power generating unit must synchronize
Upper dedusting, desulphurization and denitration device, and the flue gas ash removal of in-service fired power generating unit, desulphurization and denitration device then should by renovation and improving, with
Reduce the Air Pollutant Emission concentration of fired power generating unit.
Boiler smoke removes nitrogen oxides through SNCR-SCR combined denitration devices and then reduces cigarette by air preheater
Temperature degree is generally dropped down to from the boiler smoke temperature of air preheater outlet discharge between 120 DEG C~160 DEG C；Work as boiler
When normal operation, boiler smoke temperature is generally lowered into 130 DEG C or so.It uses the unit of middle low-sulfur coal in order to reduce or has in stove
The sulfur oxides emissions concentration of the Properties of CFB of desulfurization, in water-deficient area, people are generally using flue gas circulating fluidized bed de-
Sulphur technology carries out desulfurization to boiler smoke.
After the absorbent being injected into the inlet flue duct of recirculating fluidized bed absorption tower is mixed with flue gas, pass through adding for Venturi tube
Speed and suspend, form fierce turbulence state, make that there is prodigious opposite slip velocity between particle and flue gas.It is same with this
When, by water spraying atomization device spray into absorb the bottom of the tower humidification water, both can rapidly by the flue gas in recirculating fluidized bed be cooled to compared with
Good chemical reaction temperature simultaneously increases the smoke moisture in recirculating fluidized bed, and wettable absorbent and flue dust, it is thus possible to aobvious
The chemical reaction rate for accelerating the gases and calcium hydroxide such as sulfur dioxide, sulfur trioxide is write, and significantly improves the desulfurization on absorption tower
Efficiency.Absorbent and water are first either configured to absorbent slurry to be then injected directly into or spray into again after mixing with humidification water
Recirculating fluidized bed absorption tower.But, no matter using any absorbent dosing method therein, the work on recirculating fluidized bed absorption tower
It is substantially the same as principle.As flue gas rises in recirculating fluidized bed absorption tower, sulfur dioxide concentration in flue gas and other
Acidic gas concentration is lower and lower, and the moisture content of absorbent, desulfurizing byproduct and flue dust is then lower and lower, when close to absorption tower
When outlet, absorbent, desulfurizing byproduct and flue dust in flue gas substantially dry.It is arranged at the top of from recirculating fluidized bed absorption tower
After the flue gas gone out is purified by high-efficiency dust remover, cleaning flue gases are just discharged by chimney in air, and by high-efficiency dust remover trapping
Most of desulfurizing byproduct and the absorbent for having neither part nor lot in desulphurization reaction are then recycled back to recirculating fluidized bed absorption tower progress high magnification and follow
Ring reacts, and sub-fraction desulfurizing byproduct and the absorbent for having neither part nor lot in desulphurization reaction are just arranged by conveying equipment outside.
When using spray pattern will be humidified water spray into recirculating fluidized bed absorption tower when, it is necessary to assure absorbent in flue gas,
Substantially dry when desulfurizing byproduct and flue dust are exported close to absorption tower, and make entire desulphurization system in flue gas dew point temperature
Otherwise the above safe operation will cause the problems such as desulphurization system glues wall, high-efficiency dust remover condenses and paste bag.In actual operation,
Flue-gas temperature in recirculating fluidized bed generally should be higher than that 20 DEG C of flue gas dew point temperature or more, and the exit gas temperature one on absorption tower
As should be higher than that 15 DEG C of flue gas dew point temperature or more.
Some boilers are in summer continuous oepration at full load, as temperature increases, from the boiler smoke of air preheater out
Temperature degree also significantly increases, and leads to the import flue gas temperature on boiler smoke temperature actual value to be clean and recirculating fluidized bed absorption tower
Degree actual value is all higher by 20 DEG C or more than the input gas temperature design value on absorption tower.At this time in order to ensure in recirculating fluidized bed
Flue-gas temperature is only higher by 20 DEG C~30 DEG C than flue gas dew point temperature, so that the sour gas such as sulfur dioxide, sulfur trioxide and hydrogen-oxygen
Change calcium rapidly to chemically react, be wanted so that it is guaranteed that the sulfur dioxide emissioning concentration in the exiting flue gas of absorption tower meets design
Ask, then need to significantly increase the humidification water flow for spraying into absorption tower --- substantially it is exactly to need to significantly increase to spray into absorption tower
Be humidified water flow（Unit：Kilograms Per Second）With the ratio of absorption tower import flue gas flow.
Of course, flue gas circulating fluidized bed simultaneous SO_2 and NO removal technical finesse boiler smoke can also be used, that is, cancels pot
SNCR-SCR combined denitration devices in kiln gas purification system, and utilize and be added in recirculating fluidized bed absorption tower or follow
Denitration additive in the inlet flue duct of ring fluid bed absorption tower, first makes a part of nitric oxide in flue gas be catalytically oxidized to two
Nitrogen oxide, then in these nitrogen dioxide and flue gas the gases such as original nitrogen dioxide, sulfur dioxide and sulfur trioxide together with
The reaction of ionic type of gas-solid-liquid three-phase occurs for the calcium hydroxide in absorbent, generates calcium sulfite, calcium sulfate and calcium nitrate
Etc. compounds, to realizing flue gas and desulfurizing and denitrifying in absorption tower；The denitration additive contains potassium permanganate or Asia
Sodium chlorate or calcium hypochlorite.Or using the low temperature catalyst being mounted in the inlet flue duct of recirculating fluidized bed absorption tower, first make
A part of nitric oxide in flue gas is catalytically oxidized to nitrogen dioxide, then original dioxy in these nitrogen dioxide and flue gas
Change the ion that gas-solid-liquid three-phase occurs with the calcium hydroxide in absorbent together for the gases such as nitrogen, sulfur dioxide and sulfur trioxide
Type reacts, and generates the compounds such as calcium sulfite, calcium sulfate and calcium nitrate, to realize that flue gas simultaneous desulfurization is de- in absorption tower
Nitre.
By reading the 8th phase in 2015《Glass》In paper《Glass furnace fume catalysis oxidation absorption process（COA）Denitration
Technology pilot effect analysis》, and《9th China Steel nd Annual Meeting collection》In paper《Calcium base recirculating fluidized bed sintering flue gas
Simultaneous SO_2 and NO removal technology》And the bibliography of entitled " Chinese low-temperature flue gas desulphurization denitration technology makes a breakthrough "
（http://www.stdaily.com/cxzg80/kebaojicui/2017-03/24/content_527 588.shtml,
2017-03-24）, we understand：Using the flue gas circulating fluidized bed simultaneous SO_2 and NO removal technique of above two, can not only handle
Boiler smoke, but also the industrial smoke that the equipment such as glass furnace and sintering machine generate at runtime can be handled.
When the rate of load condensate of boiler either miscellaneous equipment is very high, boiler or the flue-gas temperature of miscellaneous equipment discharge just compare
It is high, it is likely that can make flue-gas temperature actual value to be clean and the input gas temperature actual value on absorption tower all than absorption tower into
Mouth flue-gas temperature design value is higher by 20 DEG C or more.As using Analyss of Desulphurization Technology of Flue Gas Recirculation Fluid-bad, at this time in order to ensure to follow
Flue-gas temperature in ring fluid bed is only higher by 20 DEG C~30 DEG C than flue gas dew point temperature, so that sulfur dioxide, sulfur trioxide and two
The gases such as nitrogen oxide are rapidly chemically reacted with the calcium hydroxide in absorbent, so that it is guaranteed that in the exiting flue gas of absorption tower
Sulfur dioxide emissioning concentration and discharged nitrous oxides concentration all meet design requirement, then need to significantly increase the increasing for spraying into absorption tower
Wet water flow --- substantially it is exactly to need to significantly increase the humidification water flow for spraying into absorption tower and absorption tower import flue gas flow
Ratio.
In summary it is found that the operation conditions of the equipment such as boiler, glass furnace and sintering machine can significantly affect wait for it is net
The input gas temperature of the flue-gas temperature and recirculating fluidized bed absorption tower of change.In order to ensure recirculating fluidized bed absorption tower exiting flue gas
In sulfur dioxide emissioning concentration meet design requirement or sulfur dioxide emissioning concentration and discharged nitrous oxides concentration all meets
Design requirement then needs significantly when the input gas temperature actual value on recirculating fluidized bed absorption tower is significantly higher than its design value
The ratio for increasing the humidification water flow and absorption tower import flue gas flow that spray into absorption tower produces humidification water consumption and compares then
Big technical problem.Therefore, urgently we solve to generate because the input gas temperature on recirculating fluidized bed absorption tower is excessively high at present
The bigger problem of humidification water consumption.
Invention content
The object of the present invention is to provide a kind of flue gas purification systems utilizing technology based on fume afterheat, to solve because of cycle
The input gas temperature on fluid bed absorption tower is excessively high or and the bigger problem of humidification water consumption that generates.
To achieve the goals above, the present invention adopts the following technical scheme that：A kind of cigarette utilizing technology based on fume afterheat
Gas purification system, including recirculating fluidized bed absorption tower and be arranged recirculating fluidized bed absorption tower upstream flue gas cool-down heat exchange
Device, and the flue gas temperature rise heat exchanger in recirculating fluidized bed absorption tower downstream is set；The heat of the flue gas cool-down heat exchanger
Matchmaker's water inlet pipeline is connected to the heating agent water outlet line of the flue gas temperature rise heat exchanger, and the heat of the flue gas cool-down heat exchanger
Matchmaker's water exit conduit is then connected to the heat medium water inlet ductwork of the flue gas temperature rise heat exchanger.
Preferably, further include steam turbine condensation water- to-water heat exchanger or heat supply network return water heat exchanger；The steam turbine condensed water changes
The heating agent water outlet pipe of the heat medium water inlet ductwork of hot device or the heat supply network return water heat exchanger and the flue gas cool-down heat exchanger
Road be connected to, and the steam turbine condensation water- to-water heat exchanger or the heat supply network return water heat exchanger heating agent water outlet line then with it is described
The heat medium water inlet pipeline of flue gas cool-down heat exchanger is connected to；The condensation water inlet or described of the steam turbine condensation water- to-water heat exchanger
The heat supply network return water import of heat supply network return water heat exchanger is connected to condensed water entrance branch or heat supply network return water entrance branch, and the vapour
The condensation water out of turbine condensation water- to-water heat exchanger or the heat supply network backwater outlet of the heat supply network return water heat exchanger then go out with condensed water
Mouth branch pipe or the connection of heat supply network backwater outlet branch pipe.
Preferably, electrostatic precipitator and high-effective dust-removing are respectively arranged in recirculating fluidized bed absorption tower upstream and downstream
Device；The flue gas cool-down heat exchanger is arranged on the inlet flue duct or air inlet smoke box of the electrostatic precipitator, and the flue gas
Temperature rise heat exchanger is then arranged on the inlet flue duct or air inlet smoke box of the high-efficiency dust remover；In the flue gas temperature rise heat exchanger
On the heating agent water outlet line for condensing water- to-water heat exchanger or the heat supply network return water heat exchanger with the steam turbine, it is respectively arranged with the
One cycle pump group and second circulation pump group；The first circulation pump group and the second circulation pump group all include flowmeter, electronic
Regulating valve and frequency variable circulating pump.
Preferably, the flue gas cool-down heat exchanger, the flue gas temperature rise heat exchanger and the steam turbine condense water- to-water heat exchanger
Or the heat supply network return water heat exchanger all includes shell, heat medium water import header, heat medium water outlet header and wave-fin pipe；Institute
The water inlet and water outlet for stating wave-fin pipe are connected to the heat medium water import header and the heat medium water outlet header respectively.
Preferably, further include gas flow surveying instrument, gas temperature measuring device, composite control apparatus；The gas
Exiting flue gas flow and the recirculating fluidized bed absorption tower of the flow measurement device for monitoring the flue gas cool-down heat exchanger
Import flue gas flow；The gas temperature measuring device is for monitoring the flue gas cool-down heat exchanger, recirculating fluidized bed suction
Receive the inlet and outlet flue-gas temperature of tower and the high-efficiency dust remover；The composite control apparatus prestores the recirculating fluidized bed and absorbs
The import flue gas flow design value of tower；The first circulation pump group and the second circulation pump group and condensed water disengaging
Valve on mouth branch pipe or heat supply network return water inlet and outlet branch pipe is all controlled by the composite control apparatus.
Preferably, further include active carbon powder injection apparatus；The jet pipe of the active carbon powder injection apparatus is arranged in institute
It states in the inlet flue duct of high-efficiency dust remover.
Preferably, further include the SNCR-SCR combined denitration devices that denitration is carried out to boiler smoke.
Preferably, further include denitration additive solution storage tank and double-current spray gun body.
Preferably, low temperature catalyst is installed in the inlet flue duct on the recirculating fluidized bed absorption tower, so that in flue gas
A part of nitric oxide be catalytically oxidized to nitrogen dioxide.
A kind of flue gas purification system being utilized technology based on fume afterheat provided by the present invention, including recirculating fluidized bed are inhaled
It receives tower and the flue gas cool-down heat exchanger in recirculating fluidized bed absorption tower upstream is set, and be arranged in the recirculating fluidized bed
The flue gas temperature rise heat exchanger in absorption tower downstream；The heat medium water inlet pipeline of the flue gas cool-down heat exchanger is changed with flue gas heating
The heating agent water outlet line of hot device is connected to, and the heating agent water exit conduit of the flue gas cool-down heat exchanger then heats up with the flue gas
The heat medium water inlet ductwork of heat exchanger is connected to.
When the import flue gas flow of the exiting flue gas flow measured value and recirculating fluidized bed absorption tower of flue gas cool-down heat exchanger
When the ratio of design value is more than 75%, the composite control apparatus starts first circulation pump group, and passes through the change of first circulation pump group
Frequency circulating pump and electric control valve, it is appropriate to adjust the heating agent water flow for flowing through flue gas temperature rise heat exchanger.In this way, on the one hand passing through cigarette
Gas cooling heat exchanger Mist heat recovering, can make the exit gas temperature of flue gas cool-down heat exchanger be reduced to 105 DEG C or so, from
And ensure that the input gas temperature on recirculating fluidized bed absorption tower meets the requirement of its normal operation, and solve to absorb because of recirculating fluidized bed
The bigger technical problem of water consumption that is humidified that the input gas temperature of tower is excessively high and generates；On the other hand it is heated up by flue gas
Heat exchanger utilizes the exiting flue gas on fume afterheat heat cycles fluid bed absorption tower, can make recirculating fluidized bed absorption tower and chimney
Exit gas temperature all increase 10 DEG C or so, thus can also increase atmosphere hoist height and reduce pollutant ground it is dense
Degree.
In further technical solution, this based on fume afterheat further includes steamer using the flue gas purification system of technology
Machine condenses water- to-water heat exchanger or heat supply network return water heat exchanger.When the exiting flue gas flow measured value and recycle stream of flue gas cool-down heat exchanger
The ratio for changing the import flue gas flow design value on bed absorption tower is more than 75%, and the fume afterheat that flue gas cool-down heat exchanger is recycled
When amount is noticeably greater than flue gas temperature rise heat exchanger for heating flue gas required heat, then need steam turbine condensing water- to-water heat exchanger
Or heat supply network return water heat exchanger puts into operation, with the part of smoke waste-heat steamer recycled using flue gas cool-down heat exchanger
Machine condensed water or heat supply network return water, and ensure that the input gas temperature on recirculating fluidized bed absorption tower meets the requirement of its normal operation.
Description of the drawings
Fig. 1 is the structural schematic diagram of first embodiment of the invention.
Fig. 2 is the pipeline connecting mode schematic diagram of the flue gas waste heat utilization device in first embodiment of the invention.
Fig. 3 is the structural schematic diagram of second embodiment of the invention.
Respectively label indicates as follows in figure：1-station boiler；2-SNCR-SCR combined denitration devices；3-air preheaters；
4, the heating agent water exit conduit of 4 '-flue gas cool-down heat exchangers；5,5 '-flue gas cool-down heat exchanger；6,6 '-flue gas cool-downs exchange heat
The heat medium water inlet pipeline of device；7,7 '-electrostatic precipitator；8,8 '-cleaning flue gases recirculating gas duct；9,9 '-recirculating fluidized bed
Absorption tower；10-water spraying atomization devices；11, the damper of 11 '-cleaning flue gases recirculating gas ducts；12,12 '-high-effective dust-removing
Device；13,13 '-chimney；14,14 '-active carbon powder injection apparatus；15,15 '-flue gas temperature rise heat exchanger；16,16 '-
One cycle pump group；17,17 '-niter ash cellar；18,18 '-second circulation pump group；19-steam turbines condense water- to-water heat exchanger；19′—
Heat supply network return water heat exchanger；20-condensed water outlet stools；20 '-heat supply network backwater outlet branch pipes；21-condensed water entrance branch；
21 '-heat supply network return water entrance branch；22-low-pressure heaters；22 '-heat supply network return water main pipe valves；23-sintering machines；24-sintering
Machine large flue；25-sintering machine smoke discharging pipes；26-double-current spray gun bodies；27-frequency conversion force (forcing) pumps；28-denitration additives
Solution reservoir.
Specific implementation mode
With reference to embodiment and attached drawing, the invention will be further described.
Fig. 1 is the structural schematic diagram of first embodiment of the invention.
As shown in Figure 1, a kind of flue gas purification system utilizing technology based on fume afterheat provided by the present invention, including
SNCR-SCR combined denitrations device 2, air preheater 3, flue gas cool-down heat exchanger 5, electrostatic precipitator 7, cleaning flue gases recycling
Flue 8, recirculating fluidized bed absorption tower 9, water spraying atomization device 10, flue gas temperature rise heat exchanger 15 and steam turbine condense water- to-water heat exchanger
19, and further include niter ash cellar 17, high-efficiency dust remover 12 and active carbon powder injection apparatus 14 and gas flow measurement dress
It sets, gas temperature measuring device, composite control apparatus（It is all not shown）.It is injected into 9 inlet flue duct of recirculating fluidized bed absorption tower
Absorbent slaked lime powder mixed with boiler smoke after, suspended by the acceleration of Venturi tube, form fierce turbulence
State makes have prodigious opposite slip velocity between particle and flue gas.At the same time, it is sprayed into and recycles by water spraying atomization device 10
Flue gas in recirculating fluidized bed both can be cooled to preferably chemical reaction temperature by the humidification water of 9 bottom of fluid bed absorption tower rapidly
Spend and increase the smoke moisture in recirculating fluidized bed, and wettable calcium hydroxide and flue dust, it is thus possible to dramatically speed up titanium dioxide
The chemical reaction rate of the gases such as sulphur, sulfur trioxide and calcium hydroxide, and improve the desulfuration efficiency on absorption tower.Active carbon powder sprays
The jet pipe of injection device 14 is arranged in the inlet flue duct of high-efficiency dust remover 12；It is injected into the inlet flue duct of high-efficiency dust remover 12
Active carbon powder can adsorb dioxin, mercury and mercuric compounds in flue gas；Wherein, high-efficiency dust remover 12 is sack cleaner
Or electric-bag complex dust collector.
Flue gas cool-down heat exchanger 5 is arranged on the inlet flue duct of electrostatic precipitator 7, and flue gas temperature rise heat exchanger 15 is then arranged
On the inlet flue duct of high-efficiency dust remover 12；But, flue gas cool-down heat exchanger 5 can also change the air inlet for being located at electrostatic precipitator 7
On smoke box, and flue gas temperature rise heat exchanger 15 can then change and be located on the air inlet smoke box of high-efficiency dust remover 12.Flue gas cool-down heat exchanger 5
Heat medium water inlet pipeline 6 and flue gas temperature rise heat exchanger 15 heating agent water outlet line and steam turbine condensation water- to-water heat exchanger 19 heat
Matchmaker's water outlet line is connected to, and the heating agent water exit conduit 4 of the flue gas cool-down heat exchanger 5 then heating agent with flue gas temperature rise heat exchanger 15
The heat medium water inlet ductwork connection of water inlet pipeline and steam turbine condensation water- to-water heat exchanger 19.In flue gas temperature rise heat exchanger 15 and steamer
It is respectively arranged with first circulation pump group 16 and second circulation pump group 18 on the heating agent water outlet line of machine condensation water- to-water heat exchanger 19；The
One cycle pump group 16 and second circulation pump group 18 all include a flowmeter, an electric control valve and a frequency variable circulating pump,
To monitor and adjust the heating agent water flow for flowing through flue gas temperature rise heat exchanger 15 and steam turbine condensation water- to-water heat exchanger 19 respectively.
The condensation water inlet and condensation water out of steam turbine condensation water- to-water heat exchanger 19 pass through condensed water entrance branch 21 respectively
And condensed water outlet stool 20, condensation water inlet and condensed water outlet with low-pressure heater 22；In condensation water inlet branch
It is respectively equipped with condensed water inlet valve and condensed water outlet valve on pipe 21 and condensed water outlet stool 20.Fig. 2 is in the present embodiment
The pipeline connecting mode schematic diagram of flue gas waste heat utilization device.
Flue gas cool-down heat exchanger 5, flue gas temperature rise heat exchanger 15 and steam turbine condensation water- to-water heat exchanger 19 all include shell, heating agent
Water inlet header, heat medium water outlet header and wave-fin pipe；The water inlet and water outlet of the wave-fin pipe respectively with institute
State heat medium water import header and heat medium water outlet header connection.Flue gas cool-down heat exchanger 5 and flue gas temperature rise heat exchanger 15 are also
Equipped with the steam sootblower for carrying out soot blowing to the wave-fin pipe.Power station steam turbine Auxiliary Steam is blown to these steam
Grey device provides steam.
The gas flow surveying instrument is used to monitor the exiting flue gas flow and recirculating fluidized bed of flue gas cool-down heat exchanger 5
The import flue gas flow on absorption tower 9；The gas temperature measuring device is for monitoring flue gas cool-down heat exchanger 5, recirculating fluidized bed
The inlet and outlet flue-gas temperature on absorption tower 9 and high-efficiency dust remover 12.
The composite control apparatus prestores the import flue gas flow design value on recirculating fluidized bed absorption tower 9；Cleaning flue gases
The damper 11 of recirculating gas duct, the inlet/outlet valve of first circulation pump group 16, second circulation pump group 18 and low-pressure heater 22
Valve on the condensation water entrance branch pipe of door and steam turbine condensation water- to-water heat exchanger 19 is all by the composite control apparatus control
System.
Boiler smoke is after 2 denitration of SNCR-SCR combined denitrations device, air preheater 3 cool down, then passes through flue gas cool-down
5 further Mist heat recovering of heat exchanger；Then, boiler smoke is again through electrostatic precipitator 7, recirculating fluidized bed absorption tower 9, flue gas
Temperature rise heat exchanger 15, the processing of high-efficiency dust remover 12；Finally, whole cleaning flue gases are just discharged by chimney 13 in air, or
The cleaning flue gases of a part are discharged by chimney 13 in air, and remaining cleaning flue gases just passes through cleaning flue gases recirculating gas duct
8 are recycled back to the inlet flue duct on recirculating fluidized bed absorption tower 9.
When the import flue gas stream of the exiting flue gas flow measured value and recirculating fluidized bed absorption tower 9 of flue gas cool-down heat exchanger 5
When measuring the ratio of design value and being less than or equal to 75%, the damper 11 of cleaning flue gases recirculating gas duct will be opened or
It is in the open state, and the damper 11 for adjusting accordingly by the composite control apparatus cleaning flue gases recirculating gas duct is opened
Degree, so that the import flue gas flow measured value on recirculating fluidized bed absorption tower 9 and the ratio of its import flue gas flow design value are equal to
80% or so, it collapses a problem to avoid the occurrence of recirculating fluidized bed absorption tower.
When the import flue gas stream of the exiting flue gas flow measured value and recirculating fluidized bed absorption tower 9 of flue gas cool-down heat exchanger 5
When measuring the ratio of design value more than 75%, the composite control apparatus will close the damper 11 of cleaning flue gases recirculating gas duct,
And start first circulation pump group 16, it is appropriate to adjust then by the frequency variable circulating pump and electric control valve of first circulation pump group 16
The heating agent water flow for flowing through flue gas temperature rise heat exchanger 15, with the fume afterheat recycled using flue gas cool-down heat exchanger 5, to cycle
The exiting flue gas on fluid bed absorption tower 9 is heated.In this way, on the one hand by 5 Mist heat recovering of flue gas cool-down heat exchanger, it can
So that the input gas temperature of electrostatic precipitator 7 is reduced to 105 DEG C or so, and ensure the import cigarette on recirculating fluidized bed absorption tower 9
Temperature degree meets the requirement of its normal operation, to improve the efficiency of dust collection of electrostatic precipitator 7, and solves to absorb because of recirculating fluidized bed
The bigger technical problem of water consumption that is humidified that the input gas temperature of tower 9 is excessively high and generates；On the other hand pass through flue gas liter
The fume afterheat that warm heat exchanger 15 is recycled using flue gas cool-down heat exchanger 5, to the exiting flue gas on recirculating fluidized bed absorption tower 9 into
Row heating, the exit gas temperature of the input gas temperature and chimney 13 that make high-efficiency dust remover 12 all increase 10 DEG C or so, therefore
Not only it can avoid high-efficiency dust remover 12 and the problems such as condensing and pasting bag occurred, but also atmosphere hoist height can be increased and reduce the ground of pollutant
Face concentration.
When the import flue gas stream of the exiting flue gas flow measured value and recirculating fluidized bed absorption tower 9 of flue gas cool-down heat exchanger 5
The ratio for measuring design value is more than 75%, and the fume afterheat amount that flue gas cool-down heat exchanger 5 is recycled is noticeably greater than flue gas heating heat exchange
When device 15 is for heating flue gas required heat, then need to put into operation steam turbine condensation water- to-water heat exchanger 19 --- open
Valve on condensed water outlet stool 20 and condensed water entrance branch 21, and pass through the Inlet and outlet water of they and low-pressure heater 22
Valve, it is appropriate to adjust the condensing water flow for flowing through steam turbine condensation water- to-water heat exchanger 19；Then start second circulation pump group 18, and lead to
The frequency variable circulating pump and electric control valve of second circulation pump group 18 are crossed, it is appropriate to adjust the heat for flowing through steam turbine condensation water- to-water heat exchanger 19
Matchmaker's water flow with the part of smoke waste-heat steam turbine condensed water recycled using flue gas cool-down heat exchanger 5, and ensures to follow
The input gas temperature on ring fluid bed absorption tower 9 meets the requirement of its normal operation.
Furthermore, it is necessary to remark additionally 2 points：First, can lime slurry first be configured to for calcium hydroxide and water, then by lime
Slurries spray into 9 bottom of recirculating fluidized bed absorption tower, or after lime slurry is mixed with humidification water, then from recirculating fluidized bed absorption
9 bottom centre of tower sprays into.
Second is that it is appreciated that, it is not necessary to flue gas cool-down heat exchanger 5 exiting flue gas flow measured value with it is ciculation fluidized
When the ratio of the import flue gas flow design value on bed absorption tower 9 is more than 75%, the composite control apparatus just closes cleaning flue gases again
The damper 11 of cycle flue, and start first circulation pump group 16, but its ratio can be separately set according to actual needs,
It is not construed as limiting herein.Similarly, the import flue gas of electrostatic precipitator 7 is made to be reduced to 105 DEG C or so and make high-efficiency dust remover 12
Input gas temperature increases 10 DEG C or so, and can separately set its temperature according to actual needs.
Fig. 3 is the structural schematic diagram of second embodiment of the invention.
As shown in figure 3, another flue gas purification system that technology is utilized based on fume afterheat provided by the present invention, including
It is sintering machine smoke discharging pipe 25, flue gas cool-down heat exchanger 5 ', electrostatic precipitator 7 ', cleaning flue gases recirculating gas duct 8 ', ciculation fluidized
Bed absorption tower 9 ', flue gas temperature rise heat exchanger 15 ' and heat supply network return water heat exchanger 19 ', and further include niter ash cellar 17 ', efficiently remove
Dirt device 12 ', active carbon powder injection apparatus 14 ', double-current spray gun body 26, frequency conversion force (forcing) pump 27 and denitration additive solution storage tank
28 and gas flow surveying instrument, gas temperature measuring device, composite control apparatus（It is all not shown）.It is injected into recycle stream
After absorbent slaked lime powder in 9 ' inlet flue duct of change bed absorption tower is mixed with sintering flue gas, hanged by the acceleration of Venturi tube
It floats, forms fierce turbulence state, make that there is prodigious opposite slip velocity between particle and flue gas.At the same time, lead to
Double-current spray gun body 26 and frequency conversion force (forcing) pump 27 are crossed, water will be humidified and denitration additive solution sprays into recirculating fluidized bed absorption tower 9 '
Bottom.The denitration additive solution is liquor potassic permanganate either sodium chlorite solution or calcium hypochlorite solution.It is injected into
It is anti-both can be cooled to preferably chemistry by the humidification water of 9 ' bottom of recirculating fluidized bed absorption tower rapidly for flue gas in recirculating fluidized bed
It answers temperature and increases the smoke moisture in recirculating fluidized bed, and wettable slaked lime powder and flue dust, it is thus possible to dramatically speed up two
The chemical reaction rate of the gases such as sulfur oxide, sulfur trioxide and nitrogen dioxide and calcium hydroxide, and improve the desulfurization effect on absorption tower
Rate and denitration efficiency.
Interior on recirculating fluidized bed absorption tower 9 ', nitric oxide in flue gas is first catalytically oxidized to nitrogen dioxide, then this
The gases such as original nitrogen dioxide, sulfur dioxide and sulfur trioxide occur with calcium hydroxide together in a little nitrogen dioxide and flue gas
The reaction of ionic type of gas-solid-liquid three-phase generates the compounds such as calcium sulfite, calcium sulfate and calcium nitrate, to realize that flue gas is same
When desulphurization denitration.Then, it using the active carbon powder being injected into the inlet flue duct of high-efficiency dust remover 12 ', adsorbs in flue gas
Dioxin, mercury and mercuric compounds；Wherein, high-efficiency dust remover 12 ' is sack cleaner or electric-bag complex dust collector.
Flue gas cool-down heat exchanger 5 ' is arranged on the inlet flue duct of electrostatic precipitator 7 ', and flue gas temperature rise heat exchanger 15 ' is then
It is arranged on the inlet flue duct of high-efficiency dust remover 12 '.The heat medium water inlet pipeline 6 ' of flue gas cool-down heat exchanger 5 ' heats up with flue gas
The heating agent water outlet line connection of the heating agent water outlet line and heat supply network return water heat exchanger 19 ' of heat exchanger 15 ', and flue gas cool-down changes
The heating agent water exit conduit 4 ' of hot device 5 ' then with the heat medium water inlet ductwork of flue gas temperature rise heat exchanger 15 ' and heat supply network return water heat exchanger
19 ' heat medium water inlet ductwork connection.In the heating agent water outlet pipe of flue gas temperature rise heat exchanger 15 ' and heat supply network return water heat exchanger 19 '
Road is respectively arranged with first circulation pump group 16 ' and second circulation pump group 18 '；First circulation pump group 16 ' and second circulation pump group
18 ' all include a flowmeter, an electric control valve and a frequency variable circulating pump, to monitor respectively and adjusting flows through flue gas
The heating agent water flow of temperature rise heat exchanger 15 ' and heat supply network return water heat exchanger 19 '.
Heat supply network return water main pipe valve 22 ' is equipped in the heat supply network return water main pipe of heat supply network circulation；Heat supply network return water heat exchanger
19 ' heat supply network return water import and heat supply network backwater outlet pass through heat supply network return water entrance branch 21 ' and heat supply network backwater outlet branch pipe respectively
20 ', it is connected to the water inlet of heat supply network return water main pipe valve 22 ' and water outlet；Go out in heat supply network return water entrance branch 21 ' and heat supply network return water
Mouth branch pipe 20 ' is above respectively equipped with heat supply network return water inlet valve and heat supply network return water outlet valve.
Flue gas cool-down heat exchanger 5 ', flue gas temperature rise heat exchanger 15 ' and heat supply network return water heat exchanger 19 ' all include shell, heating agent
Water inlet header, heat medium water outlet header and wave-fin pipe；The water inlet and water outlet of the wave-fin pipe respectively with institute
State heat medium water import header and heat medium water outlet header connection.Flue gas cool-down heat exchanger 5 ' and flue gas temperature rise heat exchanger 15 '
It is further equipped with the steam sootblower that soot blowing is carried out to the wave-fin pipe.Iron company provides thermo-power station steam turbine auxiliary steam for oneself
System provides steam to these steam sootblowers.
The gas flow surveying instrument is used to monitor the exiting flue gas flow of flue gas cool-down heat exchanger 5 ' and ciculation fluidized
The import flue gas flow on bed absorption tower 9 '；The gas temperature measuring device is for monitoring flue gas cool-down heat exchanger 5 ', recycle stream
Change the inlet and outlet flue-gas temperature of bed absorption tower 9 ' and high-efficiency dust remover 12 '.
The composite control apparatus prestores the import flue gas flow design value on recirculating fluidized bed absorption tower 9 '；Cleaning flue gases
Damper 11 ', first circulation pump group 16 ', second circulation pump group 18 ' and the heat supply network return water main pipe valve 22 ' of recirculating gas duct, with
And the valve on the heat supply network return water inlet and outlet branch pipe of heat supply network return water heat exchanger 19 ' is all controlled by the composite control apparatus.
The sintering flue gas that sintering machine 23 is discharged enters sintering machine smoke discharging pipe 25 through sintering machine large flue 24, and passes through flue gas
5 ' Mist heat recovering of cooling heat exchanger；Then, sintering flue gas is again through electrostatic precipitator 7 ', recirculating fluidized bed absorption tower 9 ', cigarette
Gas temperature rise heat exchanger 15 ', the processing of high-efficiency dust remover 12 '；Finally, whole cleaning flue gases are just discharged by chimney 13 ' in air,
Or the cleaning flue gases of a part are discharged by chimney 13 ' in air, and remaining cleaning flue gases is just followed by cleaning flue gases again
Annular smoke flue 8 ' is recycled back to the inlet flue duct on recirculating fluidized bed absorption tower 9 '.
As first embodiment, when exiting flue gas flow measured value and the recirculating fluidized bed of flue gas cool-down heat exchanger 5 ' are inhaled
When receiving the ratio of the import flue gas flow design value of tower 9 ' less than or equal to 75%, the flue gear of cleaning flue gases recirculating gas duct
Plate 11 ' will be opened or in the open state, and adjust accordingly cleaning flue gases recycling by the composite control apparatus
11 ' the aperture of damper of flue, so that the import flue gas flow measured value on recirculating fluidized bed absorption tower 9 ' and its import flue gas
The ratio of flow design value is equal to 80% or so, collapses a problem to avoid the occurrence of recirculating fluidized bed absorption tower.
When the import flue gas of the exiting flue gas flow measured value and recirculating fluidized bed absorption tower 9 ' of flue gas cool-down heat exchanger 5 '
When the ratio of flow design value is more than 75%, the composite control apparatus will close the damper of cleaning flue gases recirculating gas duct
11 ', and start first circulation pump group 16 ', then by the frequency variable circulating pump and electric control valve of first circulation pump group 16 ', fit
The heating agent water flow of flue gas temperature rise heat exchanger 15 ' is flowed through when adjusting, more than the flue gas that is recycled using flue gas cool-down heat exchanger 5 '
Heat heats the exiting flue gas on recirculating fluidized bed absorption tower 9 '.In this way, on the one hand being recycled by flue gas cool-down heat exchanger 5 '
Fume afterheat can make the input gas temperature of electrostatic precipitator 7 ' be reduced to 105 DEG C or so, and ensure that recirculating fluidized bed absorbs
The input gas temperature of tower 9 ' meet its normal operation requirement, to improve the efficiency of dust collection of electrostatic precipitator 7 ', and solve because
The bigger technical problem of water consumption that is humidified that the input gas temperature on recirculating fluidized bed absorption tower 9 ' is excessively high and generates；It is another
Aspect utilizes the fume afterheat that flue gas cool-down heat exchanger 5 ' is recycled by flue gas temperature rise heat exchanger 15 ', is inhaled to recirculating fluidized bed
The exiting flue gas for receiving tower 9 ' is heated, and the input gas temperature of high-efficiency dust remover 12 ' and the exit gas temperature of chimney 13 ' are made
10 DEG C or so are all increased, therefore not only can avoid high-efficiency dust remover 12 ' and the problems such as condensing and pasting bag occurred, but also plume rise can be increased
Height and the groundlevel concentration for reducing pollutant.
When the import flue gas of the exiting flue gas flow measured value and recirculating fluidized bed absorption tower 9 ' of flue gas cool-down heat exchanger 5 '
The ratio of flow design value is more than 75%, and the fume afterheat amount that flue gas cool-down heat exchanger 5 ' is recycled is noticeably greater than flue gas heating
When heat exchanger 15 ' is for heating flue gas required heat, then need to put into operation on heat supply network return water heat exchanger 19 ' --- beat
The valve on heat supply network backwater outlet branch pipe 20 ' and heat supply network return water entrance branch 21 ' is opened, and passes through they and heat supply network return water main pipe
Valve 22 ', it is appropriate to adjust the heat supply network circling water flow rate for flowing through heat supply network return water heat exchanger 19 '；Then start second circulation pump group 18 ', and
It is appropriate to adjust the heat for flowing through heat supply network return water heat exchanger 19 ' by the frequency variable circulating pump and electric control valve of second circulation pump group 18 '
Matchmaker's water flow with the part of smoke waste-heat heat supply network return water recycled using flue gas cool-down heat exchanger 5 ', and ensures to recycle
The input gas temperature on fluid bed absorption tower 9 ' meets the requirement of its normal operation.
Further, it is also possible to low temperature catalyst is installed in the inlet flue duct on recirculating fluidized bed absorption tower 9 ', more specifically,
Low temperature catalyst is installed in the horizontal flue of 5 ' upstream of flue gas cool-down heat exchanger, so that a part of nitric oxide quilt in flue gas
It is catalytically oxidized to nitrogen dioxide, then original nitrogen dioxide, sulfur dioxide and sulfur trioxide in these nitrogen dioxide and flue gas
The reaction of ionic type of gas-solid-liquid three-phase occurs with the calcium hydroxide in absorbent together for equal gases, generates calcium sulfite, sulphur
The compounds such as sour calcium and calcium nitrate, to realize flue gas and desulfurizing and denitrifying in absorption tower.Of course, be only humidified water at this time
The bottom on recirculating fluidized bed absorption tower 9 ' is sprayed by double-current spray gun body 26.
Claims (9)
1. a kind of flue gas purification system utilizing technology based on fume afterheat, including recirculating fluidized bed absorption tower, it is characterised in that：
Further include being arranged to inhale in the recirculating fluidized bed in the flue gas cool-down heat exchanger of recirculating fluidized bed absorption tower upstream and setting
Receive the flue gas temperature rise heat exchanger in tower downstream；The heat medium water inlet pipeline of the flue gas cool-down heat exchanger exchanges heat with flue gas heating
The heating agent water outlet line of device is connected to, and the heating agent water exit conduit of the flue gas cool-down heat exchanger is then changed with flue gas heating
The heat medium water inlet ductwork of hot device is connected to.
2. a kind of flue gas purification system utilizing technology based on fume afterheat according to claim 1, it is characterised in that：Also
Water- to-water heat exchanger or heat supply network return water heat exchanger are condensed including steam turbine；The steam turbine condensation water- to-water heat exchanger or the heat supply network return
The heat medium water inlet ductwork of water- to-water heat exchanger is connected to the heating agent water exit conduit of the flue gas cool-down heat exchanger, and the steam turbine
Condense the heating agent water outlet line of the water- to-water heat exchanger or the heat supply network return water heat exchanger then heat with the flue gas cool-down heat exchanger
Matchmaker's water inlet pipeline is connected to；The condensation water inlet of the steam turbine condensation water- to-water heat exchanger or the heat of the heat supply network return water heat exchanger
The import of net return water is connected to condensed water entrance branch or heat supply network return water entrance branch, and steam turbine condensation water- to-water heat exchanger
Condense water out either the heat supply network return water heat exchanger heat supply network backwater outlet then with condensed water outlet stool or heat supply network return water
Outlet stool is connected to.
3. a kind of flue gas purification system utilizing technology based on fume afterheat according to claim 2, it is characterised in that：
Recirculating fluidized bed absorption tower upstream and downstream are respectively arranged with electrostatic precipitator and high-efficiency dust remover；The flue gas cool-down changes
Hot device is arranged on the inlet flue duct or air inlet smoke box of the electrostatic precipitator, and the flue gas temperature rise heat exchanger is then arranged
On the inlet flue duct or air inlet smoke box of the high-efficiency dust remover；In the flue gas temperature rise heat exchanger and the steam turbine condensed water
On the heating agent water outlet line of heat exchanger or the heat supply network return water heat exchanger, it is respectively arranged with first circulation pump group and second and follows
Ring pump group；The first circulation pump group and the second circulation pump group all include flowmeter, electric control valve and frequency variable circulating pump.
4. a kind of flue gas purification system utilizing technology based on fume afterheat according to claim 3, it is characterised in that：Institute
It states flue gas cool-down heat exchanger, the flue gas temperature rise heat exchanger and steam turbine condensation water- to-water heat exchanger or the heat supply network return water changes
Hot device all includes shell, heat medium water import header, heat medium water outlet header and wave-fin pipe；The water inlet of the wave-fin pipe
Mouth and water outlet are connected to the heat medium water import header and the heat medium water outlet header respectively.
5. a kind of flue gas purification system utilizing technology based on fume afterheat according to claim 4, it is characterised in that：Also
Including gas flow surveying instrument, gas temperature measuring device, composite control apparatus；The gas flow surveying instrument is for supervising
Survey the import flue gas flow of the exiting flue gas flow and the recirculating fluidized bed absorption tower of the flue gas cool-down heat exchanger；The gas
Temperature measuring device is for monitoring the flue gas cool-down heat exchanger, the recirculating fluidized bed absorption tower and the high-efficiency dust remover
Inlet and outlet flue-gas temperature；The composite control apparatus prestores the import flue gas flow design on the recirculating fluidized bed absorption tower
Value；The first circulation pump group and the second circulation pump group and the condensation water entrance branch pipe or the heat supply network return
Valve on water entrance branch pipe is all controlled by the composite control apparatus.
6. a kind of flue gas purification system utilizing technology based on fume afterheat according to claim 5, it is characterised in that：Also
Including active carbon powder injection apparatus；The import in the high-efficiency dust remover is arranged in the jet pipe of the active carbon powder injection apparatus
In flue.
7. a kind of flue gas purification system utilizing technology based on fume afterheat according to any one of claims 1 to 6,
It is characterized in that：Further include the SNCR-SCR combined denitration devices that denitration is carried out to boiler smoke.
8. a kind of flue gas purification system utilizing technology based on fume afterheat according to any one of claims 1 to 6,
It is characterized in that：Further include denitration additive solution storage tank and double-current spray gun body.
9. a kind of flue gas purification system utilizing technology based on fume afterheat according to any one of claims 1 to 6,
It is characterized in that：Low temperature catalyst is installed in the inlet flue duct on the recirculating fluidized bed absorption tower, so that one in flue gas
Part nitric oxide is catalytically oxidized to nitrogen dioxide.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112275058A (en) * | 2020-10-19 | 2021-01-29 | 昆岳互联环境技术(江苏)有限公司 | Ammonia-free desulfurization and denitrification system and desulfurization and denitrification method |
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| CN101254394A (en) * | 2008-04-25 | 2008-09-03 | 武汉凯迪电力环保有限公司 | Sintering device flue gas multiple pollutant removing process and system thereof |
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