CN106474912A - CO in a kind of flyash removing power-plant flue gas2Device and method - Google Patents
CO in a kind of flyash removing power-plant flue gas2Device and method Download PDFInfo
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- CN106474912A CN106474912A CN201610991089.1A CN201610991089A CN106474912A CN 106474912 A CN106474912 A CN 106474912A CN 201610991089 A CN201610991089 A CN 201610991089A CN 106474912 A CN106474912 A CN 106474912A
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- flyash
- flue gas
- fluid bed
- removing power
- pipe laying
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- 239000010881 fly ash Substances 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000003546 flue gas Substances 0.000 claims abstract description 51
- 239000012530 fluid Substances 0.000 claims abstract description 40
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000002956 ash Substances 0.000 claims abstract description 11
- 238000001994 activation Methods 0.000 claims abstract description 10
- 239000000843 powder Substances 0.000 claims abstract description 10
- 238000012546 transfer Methods 0.000 claims abstract description 8
- 238000006243 chemical reaction Methods 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 18
- 230000005684 electric field Effects 0.000 claims description 17
- 239000007787 solid Substances 0.000 claims description 14
- 239000007789 gas Substances 0.000 claims description 13
- 239000000779 smoke Substances 0.000 claims description 13
- 230000000694 effects Effects 0.000 claims description 10
- 230000004913 activation Effects 0.000 claims description 7
- 238000006477 desulfuration reaction Methods 0.000 claims description 4
- 230000023556 desulfurization Effects 0.000 claims description 4
- 230000005611 electricity Effects 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 235000019504 cigarettes Nutrition 0.000 claims description 3
- 210000000031 electric organ Anatomy 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 238000012913 prioritisation Methods 0.000 abstract description 2
- 239000003245 coal Substances 0.000 abstract 1
- 238000005261 decarburization Methods 0.000 description 9
- 230000008569 process Effects 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 5
- 241000196324 Embryophyta Species 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 5
- 230000009471 action Effects 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 239000002910 solid waste Substances 0.000 description 5
- 230000004888 barrier function Effects 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 239000012159 carrier gas Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000005243 fluidization Methods 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 239000003513 alkali Substances 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 239000003500 flue dust Substances 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 150000008064 anhydrides Chemical class 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 229960004424 carbon dioxide Drugs 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 239000010883 coal ash Substances 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000037452 priming Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 238000005034 decoration Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving 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
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- 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
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses CO in a kind of removing power-plant flue gas using flyash2Device, including activated reactor, charge device, fluid bed, cyclone separator, reject bin；The activated reactor output end connects charge device；The output end connection fluid bed of the charge device；The fluid bed output end connects cyclone separator；The cyclone separator output end connects reject bin.The invention also discloses CO in a kind of removing power-plant flue gas using flyash2Method, comprise the following steps：Ash transfer is carried out activation process in activated reactor, being delivered to powder charge device afterwards carries out on-line treatment, be then sent in fluidized bed plant CO in removing flue gas2, finally deliver to reject bin.Apparatus of the present invention are organically combined with coal generating system, are provided thermal source and low-temperature receiver using coal-fired plant flue gas and cold air for device, and are passed through thermoelectric generation electric energy for needed for device offer, are a kind of prioritization schemes of reduces cost and energy consumption.
Description
Technical field
The present invention relates to solid waste resource recovery is utilized and pollution reduction field during using energy source, more properly
Say, be related to CO in a kind of removing power-plant flue gas using flyash2Devices and methods therefor, belong to collecting carbonic anhydride and reduce discharging skill
Art field.
Background technology
CO2Trapping is control coal-burning power plant CO2The effective way of discharge.CO is trapped from coal-fired plant flue gas2Technology road
Line is numerous, can totally be divided into：Decarburization and post-combustion capture in pre-combustion capture, burning.CO after burning2Trapping technique is because having not
Impact upstream combustion technical process, and not by CO in flue gas2Concentration affects, excellent without the need for carrying out transforming etc. to existing electric power factory equipment
Gesture, can be directly used for CO in traditional coal-fired plant flue gas2Separate.
CO after the more ripe burning of business application2Trapping technique is mainly liquid amine method and heat alkali liquid method.Although liquid amine
Method and heat alkali liquid method have the advantages such as high, the renewable and system stability of decarburization efficiency, and which also exposes regeneration in application process
High energy consumption, alkali lye corrosive equipment, secondary pollution and the defect such as equipment investment and system operation cost height.
CO in flue gas after being burnt by gas-solid reaction using alkali metal base absorbant2Trapping technique has energy consumption of reaction
Low, the advantages of recycle efficiency high, non-secondary pollution corrosion-free to equipment, it is considered to be the new technology of great development prospect.
But it is used for CO2The factors such as the raw material sources of the solid absorbent of trapping, cost and preparation technology constrain which to a certain extent
Large-scale application in coal-fired plant flue gas decarburization.The coal-burning power plant CO of exploitation high efficiency, low energy consumption and low cost2Solid sorbent
Agent is imperative.
In recent years, CO in flue gas after industrial solid castoff is applied to burn2The research of trapping receives much concern.In flyash
Rich in active tephre material, it is one of typical industrial solid castoff.Using in flue gas after flyash removing burning
CO2, on the one hand can achieve solid waste resource recovery and utilize, the pollution problem that its landfill disposal is brought is solved, on the other hand may be used
The preventing and treating of coal-fired flue-gas pollutant is realized, and with larger economic benefit, is expected to new way be opened up for alleviating greenhouse effects.
At present, flyash removing combustion product gases CO2Approach mainly have three classes：In flyash CaO containing active component and
MgO, can CO in Direct Acquisition flue gas under the high temperature conditions2；SiO containing active component in flyash2, silicate thing phase is can extract,
Under hot conditions directly with CO in flue gas2Reaction；To flyash surface preparation and basic group modification can be added, in middle low temperature
Under the conditions of trap flue gas in CO2.Research shows that above-mentioned three kinds of methods all can achieve flyash to CO in combustion product gases2Trapping.
But the utilization ratio of flyash is low, decarbonization process high energy consumption, system need to be optimized further.
Content of the invention
Goal of the invention：The technical problem to be solved is for the deficiencies in the prior art, provides one kind and utilizes work
CO in industry solid waste coal ash removing power-plant flue gas2Device, realize collecting carbonic anhydride and solid waste resource recovery
Utilize.
In order to solve above-mentioned technical problem, the invention discloses CO in a kind of removing power-plant flue gas using flyash2Dress
Put, it is characterised in that including activated reactor, heating pipe laying, thermoelectric generator, transformer, charge device, electrode wires, electrode
Plate, fluid bed, radiating pipe laying, cyclone separator and reject bin；The activated reactor input sends into flyash, output end
Connection charge device；The output end connection fluid bed of the charge device；The fluid bed output end connects cyclone separator；Institute
State cyclone separator lower output side connection reject bin top.
In the present invention, heating pipe laying is set in the activated reactor, the exothermic medium in buried tube type heater be from
The high-temperature flue gas of boiler superheater front end smoke canal, are used for and boiler air after heating pipe laying outlet one thermoelectric generator of connection
Preheater front end smoke canal connects, and high-temperature flue gas are re-fed into boiler air preheater front end smoke canal after lowering the temperature in heating pipe laying.
In the present invention, the charge device is connected with activated reactor output end, and the flyash after activation is input into charged dress
Putting carries out charged process, and the electric energy of the charge device is provided by thermoelectric generator.
In the present invention, radiating pipe laying in the fluid bed, is set, the heat-absorbing medium in buried tube type radiator is from air preheat
Tributary cold air in device air blast.The radiating pipe laying be connected to after thermoelectric generator for boiler air preheater air blast
Tributary cold air connection in machine, cold air are re-fed into boiler air preheater entrance after heating in buried tube type radiator.
In the present invention, battery lead plate in the fluid bed, is set, battery lead plate forms electric field, the electricity of the battery lead plate in fluid bed
Can be provided by thermoelectric generator.
In the present invention, in the activated reactor, after heating imbedded pipe heat-exchanging, flue gas is empty after heating up with radiating pipe laying in fluid bed
Gas flows separately through thermoelectric generator, and thermoelectric generator is generated electricity using the system temperature difference.
In the present invention, between the charge device and thermoelectric generator, transformer is provided with.
The invention also discloses CO in a kind of removing power-plant flue gas using flyash2Method, comprise the following steps：To receive
The ash transfer of collection carries out activation process in activated reactor, and after activation, ash transfer is carried to powder charge device
Electric treatment forms the powered flyash of high activity, is then sent in fluidized bed plant and the cigarette after the desulfurization of fluid bed bottom input
CO in solid/liquid/gas reactions removing flue gas2, reacted flyash is transported to cyclone separator and carries out gas solid separation, the flyash after separating
Being delivered to reject bin waits next step to process, and tail gas enters chimney and is expelled directly out.
Beneficial effect：
1st, device of the present invention removes CO in power-plant flue gas by the use of flyash as solid absorbent2, can turn waste into wealth,
Solid waste resource recovery utilization is realized, is conducive to saving system cost.Additionally, system decarburization efficiency is high, energy consumption is low, to equipment
Corrode little, equipment and operating cost is low, be efficient and the prioritization scheme of energy-conserving and environment-protective.
2nd, the present invention is drawn high-temperature flue gas by coal-burning boiler superheater front end smoke canal, is provided activation using heating pipe laying
Energy needed for reaction, fully reclaims and utilizes residual heat of electric power plant resource, improve the economy of system operation.Device of the present invention
Using radiating pipe laying, by cold air being drawn in air preheater air blast as heat eliminating medium, maintain fluid bed interior reaction temperature
Constant, it is ensured that flyash decarburizing reaction is effectively carried out；Decarburizing reaction heat release is utilized effectively, and improves the economy of system operation
Property.
3rd, charge device simple structure of the present invention, running resistance are little, and equipment energy consumption is low.Device adopts " honeycomb " shape structure,
Powder transport path is extended, makes the powder can be fully charged under electric field action；Thermoelectric generator can as charge device power supply,
Achieve electric energy saving；Charge device is divided into ash bucket and is easy to powder to enter fluidized bed.
4th, fluid bed inwall of the present invention arranges electric field, changes flyash flow behavior in fluid bed, makes carrier gas carry flue dust
Steadily fluidize in fluid bed.
Description of the drawings
With reference to the accompanying drawings and detailed description the present invention is done and further illustrate, the present invention's is above-mentioned
And/or otherwise advantage will become apparent.
Fig. 1 is the overall structure diagram of apparatus of the present invention.
Specific embodiment
The present invention is elaborated below in conjunction with accompanying drawing.
Such as Fig. 1, apparatus of the present invention equipment include activated reactor 1, heating pipe laying 2, thermoelectric generator 3, transformer 4, lotus
Electric installation 5, electrode wires 6, battery lead plate 7, fluid bed 8, radiating pipe laying 9, cyclone separator 11 and reject bin 10.Matter Transfer bag
Include：Flue gas C after high-temperature flue gas A, flyash B, heat exchange from boiler superheater front end smoke canal, air returns to sky after heat absorption heats up
Air preheater air intake D, activation after flyash E, the powered flyash F of high activity, flue gas after desulfurization G, quoted from air preheater
Tributary cold air H in air blast, heat absorption heat up after air I, flyash J after decarburization, flue gas K after decarburization, flue gas is returned after heat exchange
To boiler air preheater front end smoke canal L.
As shown in figure 1, one embodiment of the present invention, the device includes activated reactor 1, heating pipe laying 2, thermo-electric generation
Device 3, transformer 4, charge device 5, electrode wires 6, battery lead plate 7, fluid bed 8, radiating pipe laying 9, cyclone separator 11, reject bin
10.1 output end of the activated reactor connects charge device 5；5 output end of the charge device connects fluidized-bed reactor 8；Institute
State 8 output end of fluidized-bed reactor connection cyclone separator 11；On 11 lower output side of the cyclone separator and reject bin 10
Portion connects；Heating pipe laying 2 is buried in the activated reactor 1 and connects boiler superheater front end smoke canal A, for cyclic high-temperature flue gas
Activation evergy is provided；The tributary H that radiator coil tube 9 connects in air preheater air blast is buried in the fluid bed 8, for circulating
Cold air medium maintains 8 temperature constant of fluid bed；Electrode wires 6 are set in the charge device 5, powered for carrying out to flyash B
Process；Battery lead plate 7 is set in the fluid bed 8, in bed body, form electric field, it is ensured that carrier gas carries flue dust steady flow in the fluid bed
Change；The thermoelectric generator 3 configures transformer 4, using system thermo-electric generation.
More specifically, activated reactor 1 is main is made up of reaction bed and heating pipe laying 2.The poling processing technique is
High activity basic anhydride are formed under basic anhydride in flyash catalyst action in the reactor, needed for priming reaction
Temperature is 600-1000 DEG C.High-temperature flue gas A is drawn by coal-burning boiler superheater front end smoke canal, flowing through described heating pipe laying 2 is
Reactor provides energy makes which maintain priming reaction temperature.The heating pipe laying 2 outlet is connected with air preheater front end smoke canal L
Connect, flue gas after heat exchange is returned boiler flue.
Charge device 5 adopts pipe-type electrostatic principle of device, is mainly made up of charge device, electric supply installation, insulating barrier etc..
The design of 5 upper and lower side of the charge device is tapered, referred to as " ash bucket ".Rapping motor is housed on " ash bucket " tube wall.Described
5 external form of charge device is cylindrical, with cylinder unit as elementary cell, inside sets multiple electrodes line side by side, in dense cellular shape.Institute
State outside cylinder unit and be made up of metal skin, colelctor electrode is constituted, cylinder unit inside center axis suspends corona wire.Electrode wires with
Install cylindrical plastic insulating barrier between device wall additional, its diameter is close to metal pipe-wall but does not fit therewith.Multiply plain conductor exists
Device outer type becomes one, is connected with transformer outlet negative pole.The positive wire connected on colelctor electrode is converged into outside device
One, is connected with transformer outlet positive pole.All insulating barriers all extend to device bottom, constitute closing space with bottom.Institute
The Charging Techniques for stating charge device are：Apply DC high-voltage power supply to charge device, set up between colelctor electrode and corona wire non-
Uniform electric field.The electric energy that the DC high-voltage power supply is produced by thermoelectric generator is provided after transformer transformation.In each cylinder
In device, nearby field intensity is maximum for corona wire connected with negative pole.Change the electric-field intensity around corona wire by adjusting voltage.When
The electric-field intensity of in the air is more than its breakdown electric field critical value, and air is breakdown to be ionized, and forms substantial amounts of negative ions.With
This simultaneously, flyash via on device side opening enter cylinder unit, collide with the anion drifted about to cathode metal plate,
Fly ash grain absorption electronics is in electronegativity.Under electric field action, the powder granule in electronegativity can be moved to positive plate, reached
During ambroin dividing plate, all charged powders are intercepted by dividing plate.Under the graviational interaction of positive plate, flyash " absorption " is exhausted
On edge plastic septum, so as to avoid, flyash institute is electrically charged to be neutralized by positive plate.At the same time, operate rapping motor, makes attached
Charged powder of the collection on insulating barrier comes off, and is entered in device lower end " ash bucket ", in case next stepping under gravity
Fluidized bed carries out CO2Removing.
Fluidized-bed reactor is characterised by：Conventional fluidization bed adopts single air feed, and carrier gas carries solid particle and exists
Bed is inner circulation fluidized, technical process high energy consumption, and noise is big, fluid bed serious wear.Behaviour of the present invention based on conventional fluidization bed
Innovation transformation is carried out as mode, electric field driven solid particle suspension fluidization is simultaneously introduced in air feed.The fluid bed inwall
And upper and lower ends are equipped with battery lead plate, apply DC high-voltage power supply to fluidized bed plant, in bed, produce electric field.Through on-line treatment
Flyash afterwards is in electronegativity, mixes with the coal-fired flue-gas for introducing after entering fluidized bed, fluidizes in electric field force effect low suspension, from
And realize CO in flue gas2Removing.The ciculation fluidized effect can adjust electric field force realization by changing magnitude of voltage.Magnitude of voltage is got over
Height, electric-field intensity are bigger, and the fluid effect of flue dust is better.When air-flow passes through fluid bed with friction speed, solid particle can be presented
Different flow regimes.When air-flow velocity reaches critical fludization velocity, solid material is moved up and down in the form of cluster of grains, is produced
The back-mixing of height.Under this flow conditions, carrier gas can carry fume gases in the fluid bed smooth outflow and with charged flyash
Mixing.Under the double action of import air blast and electric field force, above-mentioned Dual-Phrase Distribution of Gas olid assumes fluidization campaign.Ciculation fluidized
During, the powered flyash adsorption CO of high activity2, so as to realize CO in flue gas2Trapping.Gas-solid fluidized can make flyash
Decarburizing reaction more abundant, improve CO2Arresting efficiency.
The powered flyash adsorption CO of high activity2Process be heat-producing chemical reaction, it is 40- that its reaction temperature is interval
100℃.In actual decarbonizing process, exothermic heat of reaction makes to heat up inside bed, and progressively disengages optimal reaction temperature interval, causes
Flyash decarburization efficiency reduces.Radiating pipe laying is set in the fluid bed, is made with the cold air from air preheater air intake
For cooling medium, lowered the temperature for bed by circulating cold air heat absorption, to maintain decarburization temperature in optimum temperature is interval, improve powder
The decarburization efficiency of coal ash.
The operation principle of the thermoelectric generator is：Heating pipe laying is set in the activated reactor, with from boiler overheating
The high-temperature flue gas of device front end smoke canal, as thermal source, are that activated reactor intensification provides energy.After heat exchange, flue gas flows through thermo-electric generation
Air preheater flue front end transported to by device.Radiating pipe laying is set in the fluid bed, with the cold sky in tributary in boiler blower
Gas as cooling medium, to carry decarburizing reaction heat release in fluid bed.After intensification, air flows through thermoelectric generator and is transported to air
Preheater air intake front end.The fluid bed surface configuration temperature sensor, controls bed by adjusting cooling working medium flow
Temperature stabilization.The thermoelectric generator, the temperature difference (the heat exchange cigarette produced using the heat transferring medium between fluid bed and activated reactor
Gas and the temperature difference of liter warm air) generate electricity.In actual application, multiple PN junctions can be connected or by multiple thermoelectric generator strings
Connection is to improve output voltage and power output.The electric energy that the thermoelectric generator is produced is used for charge device and fluid-bed electrode
Plate.
The present invention provides CO in a kind of flyash removing power-plant flue gas2Method, its technological process is：Flyash is through making a living
After change reactor is activated, charge device is transported to.Electrode wires are set in charge device, make air ionization that negative ions are produced,
So that flyash is powered.Powered flyash is transported in fluidized-bed reactor.Flue gas after desulfurization is introduced through fluid bed low side,
Steadily fluidize with powered flyash under the electric field action that the battery lead plate is produced, the powered flyash of high activity is reacted with smoke contacts
Removing CO2.Reacted flyash is entered in reject bin after gas solid separation in cyclone separator and is stored, with to be utilized.
The invention provides CO in a kind of removing power-plant flue gas using flyash2The thinking of device and method, concrete real
Now a lot, the above is only the preferred embodiment of the present invention for the method for the technical scheme and approach, it is noted that for this
For the those of ordinary skill of technical field, under the premise without departing from the principles of the invention, some improvement and profit can also be made
Decorations, these improvements and modifications also should be regarded as protection scope of the present invention.In the present embodiment, clearly not each part all can use
Prior art is realized.
Claims (8)
1. one kind is using CO in flyash removing power-plant flue gas2Device, it is characterised in that including activated reactor (1), charged
Device (5), fluid bed (8), cyclone separator (11) and reject bin (10)；
Activated reactor (1) input sends into flyash, output end connection charge device (5)；
Output end connection fluid bed (8) of charge device (5)；
Fluid bed defeated (8) go out end connection cyclone separator (11)；
Cyclone separator (11) lower output side connection reject bin (10).
2. one kind according to claim 1 is using CO in flyash removing power-plant flue gas2Device, it is characterised in that described
Heating pipe laying (2) is set in activated reactor, heats the high temperature cigarette that the exothermic medium in pipe laying (2) is in activated reactor (1)
Gas；The outlet of heating pipe laying (2) connects a thermoelectric generator (3) to be used for and external boiler air preheater front end smoke canal afterwards
Connection.
3. one kind according to claim 2 is using CO in flyash removing power-plant flue gas2Device, it is characterised in that described
Charge device (5) is connected with activated reactor (1) output end, and flyash input charge device (5) after activation carries out charged place
Reason；The electric energy of charge device (5) is provided by thermoelectric generator (3).
4. one kind according to claim 3 is using CO in flyash removing power-plant flue gas2Device, it is characterised in that described
Radiating pipe laying (9) is set in fluid bed (8), and the heat-absorbing medium radiated in pipe laying (9) is cold air；Radiating pipe laying (9) includes
The cold air interface that one is connected with boiler air preheater air blast, and one be connected to thermoelectric generator (3) afterwards be used for and pot
The interface of stove air preheater entrance connection.
5. one kind according to claim 4 is using CO in flyash removing power-plant flue gas2Device, it is characterised in that described
Battery lead plate (7) is set in fluid bed (8), battery lead plate (7) forms electric field in fluid bed (8)；The electric energy of battery lead plate (7) is by temperature
Difference electric organ (3) is provided.
6. one kind according to claim 4 is using CO in flyash removing power-plant flue gas2Device, it is characterised in that described
After in activated reactor (1), after heating pipe laying (2) heat exchange, flue gas is heated up with radiating pipe laying (9) in fluid bed (8), air flows respectively
Through thermoelectric generator (3), thermoelectric generator (3) is generated electricity using the temperature difference.
7. one kind according to claim 3 is using CO in flyash removing power-plant flue gas2Device, it is characterised in that charged
Transformer (4) is provided between device (5) and thermoelectric generator (3).
8. one kind is using CO in flyash removing power-plant flue gas2Method, it is characterised in that comprise the following steps：
The ash transfer of collection is carried out in activated reactor activation process；
Ash transfer after activation to powder charge device is carried out on-line treatment and forms the powered flyash of high activity；
By the smoke reaction after desulfurization of powered for the high activity ash transfer to fluidized bed plant with the input of fluid bed bottom, take off
Except CO in flue gas2；
Reacted flyash is transported to cyclone separator carries out gas solid separation；
By the ash transfer after separation to reject bin.
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| CN111268881A (en) * | 2020-03-11 | 2020-06-12 | 东南大学 | Sludge reduction system charcoal system |
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