CN100594051C - Method of removing PM2.5 and gaseous pollutant using steam phase transition and device thereof - Google Patents
Method of removing PM2.5 and gaseous pollutant using steam phase transition and device thereof Download PDFInfo
- Publication number
- CN100594051C CN100594051C CN200710133987A CN200710133987A CN100594051C CN 100594051 C CN100594051 C CN 100594051C CN 200710133987 A CN200710133987 A CN 200710133987A CN 200710133987 A CN200710133987 A CN 200710133987A CN 100594051 C CN100594051 C CN 100594051C
- Authority
- CN
- China
- Prior art keywords
- flue gas
- gas
- washing absorption
- heat exchanger
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention relates to a method and a device which adopt steam phase changing to cooperatively remove PM2.5 and gas pollutions from a high temperature and high humidity flue gas. The invention comprises a dust catcher, a flue gas humidity regulating chamber, a condensing heat exchanger and a washing absorption tower. The method is that the flue gas enters the flue gas humidity regulating chamberafter coarse dust removing in the dust catcher, and atomized hot water is sprayed to regulate the humidity of the flue gas; after humidity regulation, the flue gas is induced into the condensing heatexchanger to reach supersaturation, and the supersaturation steam takes the PM2.5 as condensing core to generate phase changing, thus increasing the granularity of the PM2.5; then the steam enters the washing absorption tower, and in the tower, the flue gas reversely contact a middle-lower temperature alkalescent washing-adsorbing liquid to be further subject to the phase changing of the steam taking PM2.5 as condensing core, and the alkalescent washing-adsorbing is adopted for removing the growing dust-drop and gas pollutions. Taking the characteristics of the high temperature and high humidity flue gas into account, the invention adopts the steam phase changing theory to lead the PM2.5 to be condensed and to grow so as not only to cooperatively remove PM2.5 and gas pollution, but to recycle the gasifying potential heat released by steam condensing and the sensible heat caused by temperature reduction of the flue gas.
Description
One, technical field
The invention belongs to PM in the flue gas
2.5Particulate and gaseous contaminant remove technical field, PM in the hot and humid flue gas of particularly a kind of applying steam Transformation Principle cooperation-removal
2.5Method and device with gaseous contaminant.
Two, background technology
Pellet is the primary pollutant of present China city atmospheric environment, and especially wherein aerodynamic diameter is less than the PM of 2.5 μ m
2.5Pollution problem is very serious, and main cause is PM
2.5Big, easy each heavy metal species of enrichment of particulate specific area and chemical carcinogen, and conventional dedusting technology is difficult to effective capture to it, causes a large amount of PM
2.5Enter atmospheric environment.Burning is to cause PM in the atmospheric environment
2.5The main cause that content increases, control Combustion Source PM
2.5Discharging is the key issue that presses for solution, and the main path that technology is delivered is that the preliminary treatment measure is set before cleaner, is removed after making it grow up into larger particles by physics or chemical action, wherein uses supersaturated vapor at PM
2.5The characteristic that the microparticle surfaces coring is condensed is to impel PM
2.5The important measures that granularity increases are particularly suitable for hot and humid flue gas environment.At present, it is more and more universal that oil burning boiler, natural gas boiler, burning method are handled solid waste (as the burning disposal of waste incineration and generating electricity, mud etc.); Because of protium content height in oil, the gas fuel, solid waste such as rubbish, mud is rich in moisture, moisture content height in the flue gas that produces causes burning, as vapour content in the natural gas boiler flue gas is 15～19% (volumn concentrations, down together), vapour content is 10～15% in the oil burning boiler flue gas, and moisture content can be up to more than 20% in the flue gas of refuse burning; Simultaneously, exhaust gas temperature is mostly more than 200 ℃.In view of vapour content and exhaust gas temperature height in fuel oil, the natural gas boiler flue gas, the external standing condensing heat exchanger of putting, the latent heat of vaporization of emitting when recycling water vapour condensation in the flue gas and the sensible heat of flue gas cool-down its objective is the recovery flue gas heat, improve boiler thermal output, do not belong to PM
2.5The control technology field.Pollutant mainly contains flue dust, SO in fuel oil, the natural gas boiler flue gas
2, NO
xDeng, because of dust concentration is low, not causing enough attention as yet, removing of gaseous contaminant mainly contains wet method, dry method, though the flue dust total mass concentration is lower than corresponding coal-fired flue-gas, smoke granularity is tiny, PM in the flue gas
2.5Concentration and coal-fired flue-gas are suitable, and are rich in organic component, and be bigger to environmental hazard.Pollutant mainly contains flue dust, heavy metal and SO in solid waste incineration such as rubbish, the mud flue gas
2, HCl, HF, NO
xEtc. the acidic gaseous pollutant, the removal of flue dust mainly utilizes sack cleaner, electrostatic precipitator, though efficiency of dust collection can be higher than 99%, for PM
25Capture rate not high, SO
2, gaseous contaminants such as HCl, HF removal mainly contain three kinds of wet methods, dry method, semidry method, heavy metal such as Cr, Cd, Ni, Pb, Se etc. mainly are enriched in the fine grained, particularly PM
2.5In, only remove the fine grained in the flue gas, could effectively remove heavy metal.At present, at above-mentioned emission source, PM still not yet in effect
2.5Remove technology and cooperation-removal PM
2.5Technology with gaseous contaminant.
Three, summary of the invention
The objective of the invention is provides a kind of applying steam Transformation Principle cooperation-removal PM at vapour content and the high characteristics of exhaust gas temperature in the solid waste incineration flue gases such as oil burning boiler, natural gas boiler and rubbish, mud
2.5Method and device with gaseous contaminant.
Technical solution of the present invention is: a kind of applying steam phase transformation cooperation-removal PM
2.5With the method for gaseous contaminant, step is:
(1) PM
2.5Coalescence grow up: hot and humid flue gas (temperature: 200～500 ℃, H
2O:10～25%) after deduster removes the thick flue dust of particle diameter 〉=2.5 μ m, enter the smoke moisture conditioning chamber, spray into atomizing hot water, utilize high-temperature flue gas to make the atomized water evaporation, moisture content increases to 15～40% in the flue gas, flue gas after the adjusting humidity enters condensing heat exchanger, and steam reaches supersaturation, and supersaturated vapor is with PM
2.5Particulate is that the nuclei of condensation undergo phase transition, and makes PM
2.5Particle size increases, quality increases;
(2) the removing of dust-laden drop and gaseous contaminant of growing up of condensing: after the last step handled, saturated or supersaturation flue gas entered washing absorption tower by condensing heat exchanger, with middle low-temperature alkali washing absorption liquid counter current contacting, on the one hand, flue gas is cooled off by humidification, and degree of supersaturation further increases, and continues to take place with PM
2.5Be the steam phase transforming process of the nuclei of condensation, remove dust-laden drop and the gaseous contaminant thereof that condenses and grow up by alkaline washing absorption liquid and efficient demister simultaneously.
A kind of applying steam phase transformation realizes cooperation-removal PM
2.5Device with the gaseous contaminant method, form by deduster, smoke moisture conditioning chamber, condensing heat exchanger, washing absorption tower, the smoke moisture conditioning chamber places between deduster exhanst gas outlet and the condensing heat exchanger gas approach, built-in atomized water nozzle, the condensing heat exchanger exhanst gas outlet is connected with the washing absorption tower gas approach, makes condensing heat exchanger internal face or wall lining, coating to have the anti-corrosion low-surface-energy material of promoting phase transformation effect and anticorrosion double effects; Washing absorption tower is spray column, tubulent contact tower, packed tower or plate columns such as rotating stream tray scrubber, sieve-plate tower, and the top is provided with efficient demister, as mesh mist eliminator, baffle plate demister, eddy flow plate demister, and preferred mesh mist eliminator.Condensing heat exchanger among the present invention is mainly as making PM
2.5The pre-processing device that condenses and grow up, its effect is equivalent to the coring condensing chamber, and simultaneously, the double as flue gas waste heat recovery equipment is to recycle the water vapour condensation is emitted in the flue gas the latent heat of vaporization and the sensible heat of flue gas cool-down.
According to the present invention, applying steam phase transformation cooperation-removal PM
2.5With the method for gaseous contaminant be: hot and humid ash-laden gas enters the smoke moisture conditioning chamber remove the thick flue dust of particle diameter 〉=2.5 μ m through deduster (as sack cleaner, electrostatic precipitator) after, spraying into particle diameter is the fine hot water mist of 20～30 μ m, utilize flue gas heat to make spray vaporization, vapour content increases to 15～40% in the flue gas; Flue gas through humidity regulation enters condensing heat exchanger, makes heat exchange medium with normal-temperature water, makes that water vapour reaches the supersaturation attitude in the flue gas, and supersaturated vapor is at PM
2.5Microparticle surfaces generation coring is condensed, and makes PM
2.5Granularity increases, quality increases, and the hot water part that heat exchange produces is made the atomized water water source, all the other recyclings for the smoke moisture conditioning chamber; Enter in the tower from washing absorption tower bottom gas approach through the saturated of condensing heat exchanger or supersaturation flue gas,, strong heat and mass transfer process takes place with middle low-temperature alkali washing absorption liquid counter current contacting; On the one hand, flue gas is cooled off by humidification, and degree of supersaturation further increases, and continues to take place with PM
2.5Particulate is the steam phase transforming process of the nuclei of condensation, removes dust-laden drop and the gaseous contaminant that condenses and grow up by alkaline washing absorption liquid and efficient demister simultaneously.
Hot and humid flue gas refers to the flue gas that solid waste incinerations such as oil burning boiler, natural gas boiler, rubbish, mud produce, and vapour content is more than 10～25% in the flue gas, and exhaust gas temperature is more than 200～500 ℃, and gaseous contaminant mainly refers to SO
2, HCl, HF, NO
xEtc. the acidic gaseous pollutant, the washing absorption liquid refers to Ca (OH)
2, CaCO
3, Na
2CO
3, alkaline solution such as NaOH, ammoniacal liquor, the weight percent concentration of solution neutral and alkali absorbent is 0.5-20%.
50～80 ℃ of washing absorption tower input gas temperatures, steam is in saturated or hypersaturated state (degree of supersaturation S 〉=1) in the flue gas, import washing absorption liquid temperature is 20～50 ℃, than low 30～60 ℃ of import cigarette temperature, to realize flue gas and to wash in the absorption liquid counter current contacting process and can continue steam to take place at PM
2.5The coring condensation process of microparticle surfaces makes PM
2.5Granularity further increases, and the operation liquid-gas ratio is controlled at 1～5L/Nm
3, the flue gas degree of supersaturation is controlled at 1.1～1.5 in the condensing heat exchanger, with main generation PM
2.5Be the process of heterogeneous nucleation of the nuclei of condensation, weaken the homogeneous NUCLEATION PHENOMENA.
Beneficial effect of the present invention is: utilizing supersaturated vapor to condense in the microparticle surfaces coring is the important measures that impel its granularity to increase, but need at first set up the supersaturated vapor environment, and simple dependence added steam or cooling way to make flue gas reach the supersaturation energy consumption too high, and be only with practical value at the higher process ability of the original water vapour content of flue gas and cigarette temperature.(water vapour content is more than 10～25% to the present invention is directed in the solid waste incineration flue gases such as fuel oil and natural gas boiler, rubbish, mud vapour content and the high characteristics of exhaust gas temperature, exhaust gas temperature is more than 200～500 ℃), before the tower that can realize dedusting and absorption gaseous contaminant simultaneously, smoke moisture conditioning chamber and condensing heat exchanger are set, in the smoke moisture conditioning chamber, spray into atomizing hot water, utilize high-temperature flue gas to make the atomized water evaporation, improve humidity of flue gas, hot water is taken from condensing heat exchanger, need not the additive decrementation energy; Make heat exchange medium with normal-temperature water, make flue gas in condensing heat exchanger, reach the supersaturation attitude, utilize supersaturated vapor at PM
2.5The microparticle surfaces coring is condensed and is impelled PM
2.5Coalescence is grown up, and the water vapour condensation is emitted in the also recyclable simultaneously flue gas the latent heat of vaporization and flue gas cool-down sensible heat realize impelling PM
2.5Coalescence is grown up and the waste heat recovery double effects; Make condensing heat exchanger inwall or wall lining, coating with anti-corrosion low-surface-energy material, can promote steam at PM on the one hand
2.5Microparticle surfaces condenses and suppresses it and condense at the condensing heat exchanger wall, and then promotes the phase transformation effect, also can solve because of SO simultaneously
3, acid contaminant dewfall such as HCl and the etching problem that causes.Saturated flue gas through condensing heat exchanger enters washing absorption tower, by the reasonable adjusting import flue gas and the washing absorption liquid temperature difference, makes Ta Nei can continue to take place PM
2.5Growth process and then raising PM condense
2.5Removal effect, and remove dust-laden drop and the gaseous contaminant that condenses and grow up by alkaline detergent solution.Technology of the present invention is simple, only needs to set up smoke moisture conditioning chamber and condensing heat exchanger before existing gaseous contaminant wet method removes device-tower, can realize PM
2.5Efficiently remove with the collaborative of gaseous contaminant, and can remove the heavy metal that is enriched in the fine grained, can be widely used in the improvement of pollutant in all kinds of hot and humid flue gases.
Four, description of drawings
Fig. 1 is an apparatus structure schematic diagram of the present invention;
Fig. 2 is a process FB(flow block) of the present invention.
Among the figure: the 1-deduster; 2-smoke moisture conditioning chamber; 3-atomized water nozzle; The 4-condensing heat exchanger; The 5-washing absorption tower; 6-washing absorption liquid nozzle; The efficient demister of 7-; The 8-circulating pump
Five, the specific embodiment
As shown in Figure 1, applying steam phase transformation cooperation-removal PM of the present invention
2.5With the device of gaseous contaminant method, mainly form by deduster 1, smoke moisture conditioning chamber 2, condensing heat exchanger 4, washing absorption tower 5; Smoke moisture conditioning chamber 2 places between deduster 1 exhanst gas outlet and condensing heat exchanger 4 gas approach, and humidity regulation chamber 2 sizes are evaporated definite fully according to the water droplets that sprays into, in establish atomized water nozzle 3; Condensing heat exchanger 4 exhanst gas outlets are connected with washing absorption tower 5 gas approach, make condensing heat exchanger 4 internal faces or wall lining, coating to have the anti-corrosion low-surface-energy material of promoting phase transformation effect and anticorrosion double effects; Washing absorption tower 5 can adopt plate columns such as rotating stream tray scrubber, sieve-plate tower, and packed tower, tubulent contact tower, spray column etc., efficient demister 7 and washing absorption liquid nozzle 6 are set in the tower, and demister 7 can adopt mesh mist eliminator, baffle plate demister, eddy flow plate demister, preferred mesh mist eliminator.
As shown in Figure 2, applying steam phase transformation cooperation-removal PM
2.5With the method for gaseous contaminant be: hot and humid flue gas (water vapour content 10～25%, temperature: 200～500 ℃) after deduster 1 removes the thick flue dust of particle diameter 〉=2.5 μ m, enter smoke moisture conditioning chamber 2, spray into the fine hot water mist that particle diameter is 20～30 μ m through atomized water nozzle 3, utilize flue gas heat to make fine water-spray evaporation fully in humidity regulation chamber 2, the atomized water addition increases to 15～40% by flue gas water vapour content after regulating by 10～25% and determines; High wet flue gas through humidity regulation enters condensing heat exchanger 4, makes heat exchange medium with normal-temperature water, makes flue gas reach the supersaturation attitude, by regulating in the cooling water inflow control condensing heat exchanger 4 the flue gas degree of supersaturation 1.1～1.5, to guarantee PM
2.5Condense dust-laden size droplet diameter after growing up more than 3～5 μ m, should weaken the homogeneous NUCLEATION PHENOMENA simultaneously, make in the condensing heat exchanger 4 and mainly take place with PM
2.5Particulate is the process of heterogeneous nucleation of the nuclei of condensation; The hot water part that heat exchange produces is made the atomized water water source, all the other recyclings for smoke moisture conditioning chamber 2.Enter in the tower by washing absorption tower 5 bottom gas approach through the saturated of condensing heat exchanger 4 or supersaturation flue gas, with middle low temperature Ca (OH) through circulating pump 8,6 ejections of washing absorption liquid nozzle
2, CaCO
3, NaOH, Na
2CO
3Or alkaline solution counter current contacting such as ammoniacal liquor, the washing absorption tower input gas temperature is controlled at 50～80 ℃, is saturated or supersaturation attitude (S 〉=1), Ca (OH)
2, NaOH, Na
2CO
3Or the inlet temperature of alkaline solution such as ammoniacal liquor is controlled at 20～50 ℃, than low 30～60 ℃ of import cigarette temperature, makes in saturated flue gas and the washing absorption liquid counter current contacting process and cooled off by humidification, and degree of supersaturation further increases, and continues to take place with PM
2.5Be the steam phase transforming process of the nuclei of condensation, the operation liquid-gas ratio is controlled at 1～5L/Nm
3The dust-laden drop and the SO that condense and grow up
2, acidic gaseous pollutants such as HCl, HF are by Ca (OH)
2, CaCO
3, NaOH, Na
2CO
3Or alkaline washing absorption liquid such as ammoniacal liquor and efficient demister remove, and purifies flue gas and discharge from the cat head exhanst gas outlet.
The invention will be further described below in conjunction with embodiment, but the present invention is not only limited to this embodiment.
Flue gas is produced by fully automatic oil-fired boiler, and exhaust gas volumn is 65Nm
3/ h, water vapour content is 12% in the flue gas, 282 ℃ of exhaust gas temperatures, dust concentration peak value particle diameter are 0.07 μ m, and be most of between 0.03～0.5 μ m, SO in the flue gas
2Concentration is 624mg/Nm
3The wet scrubbing tower adopts the spray column of tower diameter 150mm, tower height 1500mm, and mesh mist eliminator is installed at the spray column top, and the washing absorption liquid is Ca (OH)
2Suspension.The ash-laden gas that oil burning boiler produces directly enters the humidity regulation chamber, by atomizer spray into 70 ℃ of temperature, particle diameter is the fine water-spray of 20～30 μ m, straying quatity is every Nm
3Flue gas 0.01kg, after regulating, outlet flue gas water vapour content increases to 24%, and temperature is 235 ℃; Enter the shell and tube condensing heat exchanger of inner liner polytetrafluoroethylene then, by regulating cooling water inflow, the flue gas degree of supersaturation is controlled at 1.2～1.3 in the condensing heat exchanger; Washing absorption tower import cigarette temperature is 65 ℃, and steam is in saturation state in the flue gas, Ca (OH)
2The suspension inlet temperature is 30 ℃, contacts liquid-gas ratio 2.5L/Nm with flue gas adverse current
3Claim low pressure impactor ELPI on-line testing through electricity, PM
2.5The mass concentration removal efficiency is 82%, and number concentration removal efficiency is 67%, and smoke desulfurization efficiency is 83%.
Except that following variation, all the other are with embodiment 1.
Washing absorption tower adopts rotating stream tray scrubber, built-in 3 blocks of eddy flow plates, and eddy flow plate demister is installed at the top, and the washing absorption liquid is Na
2CO
3Solution, liquid-gas ratio 3.5L/Nm
3After tested, PM
2.5The mass concentration removal efficiency is 86%, and number concentration removal efficiency is 72%, and smoke desulfurization efficiency is 89%.
Flue gas is produced by waste incineration, and exhaust gas volumn is 70Nm
3/ h, water vapour content is 21% in the flue gas, 243 ℃ of temperature, SO in the flue gas
2, HCl, HF concentration be respectively 729mg/Nm
3, 876mg/Nm
3, 21mg/Nm
3, deduster outlet dust concentration peak value particle diameter is 0.7 μ m, number concentration is 10
6Individual/cm
3Washing absorption tower is the rotating stream tray scrubber of tower diameter 150mm, tower height 1500mm, built-in 3 blocks of eddy flow plates, and eddy flow plate demister is installed at the top, and the washing absorption liquid is Na
2CO
3Solution.Flue gas of refuse burning enters the humidity regulation chamber after cyclone dust collectors remove thick flue dust, by atomizer spray into 65 ℃ of temperature, particle diameter is the fine water-spray of 20～30 μ m, straying quatity is every Nm
3Flue gas 0.008kg, after regulating, water vapour content increases to 27% in the outlet flue gas, and temperature is 225 ℃, enters the shell and tube condensing heat exchanger of inner liner polytetrafluoroethylene then, regulates the interior flue gas degree of supersaturation of cooling water inflow control condensing heat exchanger 1.2～1.3; Washing absorption tower import cigarette temperature is 67 ℃, and water vapour is in saturation state in the flue gas, Na
2CO
3The solution inlet port temperature is 30 ℃, and liquid-gas ratio is 3.5L/Nm
3, contact with flue gas adverse current.Claim low pressure impactor ELPI on-line testing through electricity, PM
2.5The mass concentration removal efficiency is 90%, and number concentration removal efficiency is 78%, SO
2Removal efficiency is 88%, and the HCl removal efficiency is 92%, and the HF removal efficiency is 91%.
Embodiment 4: hot and humid flue gas enters the smoke moisture conditioning chamber after deduster removes the thick flue dust of particle diameter greater than 2.5 μ m, spray into atomizing hot water, utilize high-temperature flue gas to make the atomized water evaporation, improve humidity of flue gas, flue gas through humidity regulation is introduced condensing heat exchanger, with the normal-temperature water is heat-exchange medium, makes flue gas reach the supersaturation attitude, and supersaturated vapor is with PM
2.5Particulate is that the nuclei of condensation undergo phase transition, and makes PM
2.5Particle size increases; Flue gas through condensing heat exchanger is entered in the tower by washing absorption tower bottom gas approach, and with middle low-temperature alkali washing absorption liquid counter current contacting, flue gas is cooled off by humidification, continues to take place with PM
2.5Be the steam phase transforming process of the nuclei of condensation, remove the gentle attitude pollutant of dust-laden drop that condenses and grow up by alkaline washing absorption liquid and efficient demister.Hot and humid flue gas refers to the flue gas that solid waste incinerations such as oil burning boiler, natural gas boiler and rubbish, mud produce, and vapour content is 10～25% in the flue gas, and temperature is 200～500 ℃, and gaseous contaminant is the acidic gaseous pollutant.Atomizing hot water is from condensing heat exchanger, and the particle diameter of atomizing hot water is 20～30 μ m, and vapour content increases to 15～40% in the flue gas after regulating, 150～250 ℃ of temperature.The flue gas degree of supersaturation is controlled at 1.1～1.5 in the condensing heat exchanger, with main generation PM
2.5Particulate is the heterogeneous nucleating growth process of the nuclei of condensation.Washing absorption tower import flue gas is saturated or the supersaturation flue gas, 50～80 ℃ of flue-gas temperatures, and the washing absorption liquid is an alkaline solution, the absorption liquid inlet temperature is 20～50 ℃, than low 30～60 ℃ of import cigarette temperature.Alkaline solution is Ca (OH)
2, CaCO
3, Na
2CO
3, NaOH or ammoniacal liquor, the weight percent concentration of solution neutral and alkali material is 0.5-20%.
Embodiment 5: a kind of steam phase transforming cooperation-removal PM that practices
2.5Device with the gaseous contaminant method, this device comprises deduster 1, smoke moisture conditioning chamber 2, condensing heat exchanger 4 and washing absorption tower 5, smoke moisture conditioning chamber 2 is arranged between deduster 1 exhanst gas outlet and condensing heat exchanger 4 gas approach, condensing heat exchanger 4 exhanst gas outlets are connected with washing absorption tower 5 gas approach, be provided with atomized water nozzle 3 in the smoke moisture conditioning chamber 2, be provided with washing absorption liquid nozzle 6 in the washing absorption tower 5, washing absorption liquid nozzle top is provided with efficient demister 7, washing absorption liquid nozzle 6 by pipeline be located at washing absorption tower at the bottom of circulating pump link to each other.Make condensing heat exchanger internal face or wall lining, coating, preferably polytetrafluoroethylene to have the anti-corrosion low-surface-energy material of promoting phase transformation effect and anticorrosion double effects.Efficient demister 7 is mesh mist eliminator, baffle plate demister or eddy flow plate demister, preferred mesh mist eliminator.Washing absorption tower is spray column, tubulent contact tower, packed tower, rotating stream tray scrubber or sieve-plate tower.
Comparative Examples 1
Except that following variation, all the other are with embodiment 1.
Condensing heat exchanger adopts stainless steel shell and tube condensing heat exchanger, no polytetrafluoroethyllining lining; After tested, PM
2.5The mass concentration removal efficiency is 74%, and number concentration removal efficiency is 57%, and smoke desulfurization efficiency is 83%.
Comparative Examples 2
Flue gas is produced by fully automatic oil-fired boiler, and Gas Parameters, washing absorption tower and absorption liquid are with embodiment 1, and flue gas directly enters washing absorption tower without humidity regulation chamber and condensing heat exchanger preliminary treatment; After tested, PM
2.5The mass concentration removal efficiency is 31%, and number concentration removal efficiency is 19%, and smoke desulfurization efficiency is 78%.
Comparative Examples 3
Flue gas is produced by fully automatic oil-fired boiler, Gas Parameters, washing absorption tower and absorption liquid are with embodiment 1, flue gas is without the preliminary treatment of humidity regulation chamber, but directly enter condensing heat exchanger, the flue gas degree of supersaturation is controlled at 1.2～1.3 in the heat exchanger, 48 ℃ of washing absorption tower import cigarette temperature, flue gas is saturated mode; After tested, PM
2.5The mass concentration removal efficiency is 68%, and number concentration removal efficiency is 51%, and smoke desulfurization efficiency is 85%.
Comparative Examples 4
Flue gas is produced by waste incineration, and Gas Parameters, washing absorption tower and absorption liquid be with embodiment 2, and flue gas is without humidity regulation chamber and condensing heat exchanger preliminary treatment, but after cyclone dust collectors remove thick flue dust, directly enters washing absorption tower; After tested, PM
2.5The mass concentration removal efficiency is 38%, and number concentration removal efficiency is 28%, SO
2Removal efficiency is 83%, and the HCl removal efficiency is 87%, and the HF removal efficiency is 89%.
Claims (10)
1. applying steam phase transformation cooperation-removal PM
2.5Method with gaseous contaminant, it is characterized in that hot and humid flue gas enters the smoke moisture conditioning chamber after deduster removes the thick flue dust of particle diameter greater than 2.5 μ m, spray into atomizing hot water, utilize high-temperature flue gas to make the atomized water evaporation, improving humidity of flue gas, introduce condensing heat exchanger through the flue gas of humidity regulation, is heat-exchange medium with warm water, make flue gas reach the supersaturation attitude, supersaturated vapor is with PM
2.5Particulate is that the nuclei of condensation undergo phase transition, and makes PM
2.5Particle size increases; Flue gas through condensing heat exchanger is entered in the tower by washing absorption tower bottom gas approach, and with middle low-temperature alkali washing absorption liquid counter current contacting, flue gas is cooled off by humidification, continues to take place with PM
2.5Be the steam phase transforming process of the nuclei of condensation, remove the gentle attitude pollutant of dust-laden drop that condenses and grow up by alkaline washing absorption liquid and demister.
2. applying steam phase transformation cooperation-removal PM2 according to claim 1, method with gaseous contaminant, it is characterized in that described hot and humid flue gas refers to the flue gas that oil burning boiler, natural gas boiler and rubbish, sewage sludge solid castoff burning produce, vapour content is 10～25% in the flue gas, temperature is 200～500 ℃, and gaseous contaminant is the acidic gaseous pollutant.
3. applying steam phase transformation cooperation-removal PM according to claim 1
2.5With the method for gaseous contaminant, it is characterized in that described atomizing hot water from condensing heat exchanger, the particle diameter of atomizing hot water is 20～30 μ m, vapour content increases to 15～40% in the flue gas after regulating, 150～250 ℃ of temperature.
4. applying steam phase transformation cooperation-removal PM according to claim 1
2.5With the method for gaseous contaminant, it is characterized in that the flue gas degree of supersaturation is controlled at 1.1～1.5 in the described condensing heat exchanger, with main generation PM
2.5Particulate is the heterogeneous nucleating growth process of the nuclei of condensation.
5. applying steam phase transformation cooperation-removal PM according to claim 1
2.5With the method for gaseous contaminant, it is characterized in that described washing absorption tower import flue gas is saturated or the supersaturation flue gas, 50～80 ℃ of flue-gas temperatures, the washing absorption liquid is an alkaline solution, the liquid phase inlet temperature is 20～50 ℃, than low 30～60 ℃ of import cigarette temperature.
6. applying steam phase transformation cooperation-removal PM according to claim 1
2.5With the method for gaseous contaminant, it is characterized in that described alkaline solution is Ca (OH)
2Solution, CaCO
3Solution, Na
2CO
3Solution, NaOH solution or ammoniacal liquor.
7. implement the described applying steam phase transformation of claim 1 cooperation-removal PM for one kind
2.5Device with the gaseous contaminant method, it is characterized in that this device comprises deduster (1), smoke moisture conditioning chamber (2), condensing heat exchanger (4) and washing absorption tower (5), smoke moisture conditioning chamber (2) is arranged between deduster (1) exhanst gas outlet and condensing heat exchanger (4) gas approach, condensing heat exchanger (4) exhanst gas outlet is connected with washing absorption tower (5) gas approach, be provided with atomized water nozzle (3) in the smoke moisture conditioning chamber (2), washing absorption tower (5) top is provided with washing absorption liquid nozzle (6), washing absorption liquid nozzle top is provided with demister (7), washing absorption liquid nozzle (6) by pipeline be located at washing absorption tower at the bottom of circulating pump link to each other.
8. device according to claim 7 is characterized in that making condensing heat exchanger internal face or wall lining coating to have the anti-corrosion low-surface-energy material of promoting phase transformation effect and anticorrosion double effects, and described coating is polytetrafluoroethylene (PTFE).
9. device according to claim 7 is characterized in that described demister (7) is mesh mist eliminator, baffle plate demister or eddy flow plate demister.
10. device according to claim 7 is characterized in that described washing absorption tower is spray column, tubulent contact tower, packed tower, rotating stream tray scrubber or sieve-plate tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200710133987A CN100594051C (en) | 2007-10-26 | 2007-10-26 | Method of removing PM2.5 and gaseous pollutant using steam phase transition and device thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200710133987A CN100594051C (en) | 2007-10-26 | 2007-10-26 | Method of removing PM2.5 and gaseous pollutant using steam phase transition and device thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101224367A CN101224367A (en) | 2008-07-23 |
| CN100594051C true CN100594051C (en) | 2010-03-17 |
Family
ID=39856700
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200710133987A Expired - Fee Related CN100594051C (en) | 2007-10-26 | 2007-10-26 | Method of removing PM2.5 and gaseous pollutant using steam phase transition and device thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100594051C (en) |
Families Citing this family (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101732977B (en) * | 2010-01-20 | 2012-04-25 | 东南大学 | Device and method for improving fine particle removal in coal-fired flue gas desulfurization process |
| CN102059033A (en) * | 2010-12-21 | 2011-05-18 | 哈尔滨工程大学 | Condensation agglomeration trapping method and device of ultrafine particulate matter in combustion gas |
| CN102294159B (en) * | 2011-07-04 | 2014-03-26 | 中国石化集团南京化学工业有限公司 | Integrated treatment device and treatment process for tail gas containing dust and damp and hot gases |
| CN103230717B (en) * | 2013-04-26 | 2016-03-16 | 东南大学 | A kind of steam phase transformation condensation promotes the device that PM2.5 fine particle removes |
| CN104941355A (en) * | 2014-03-30 | 2015-09-30 | 天津东大化工集团有限公司 | Comprehensive recovery tower for tail gas in sodium benzoate production process |
| CN104190199B (en) * | 2014-09-02 | 2016-03-23 | 国家海洋局第三海洋研究所 | Sound wave and phase transformation coupling effect remove fine grain apparatus and method |
| CN104906913B (en) * | 2015-04-17 | 2016-08-24 | 东南大学 | A kind of method and device utilizing humidification and condensation to bear water reduction airborne suspended particulate |
| CN105013270B (en) * | 2015-06-24 | 2017-09-01 | 四川理工学院 | A kind of PM2.5 method in multistage wet method removing industrial tail gas |
| CN105536424B (en) * | 2015-12-09 | 2017-07-07 | 东南大学 | A kind of method for building up and device of steam degree of supersaturation |
| CN106076052A (en) * | 2016-07-20 | 2016-11-09 | 武汉工程大学 | A kind of atomizing air cleaning system |
| CN106582236A (en) * | 2016-12-09 | 2017-04-26 | 江苏方天电力技术有限公司 | Method and device for combined removal of SO2/NOx/PM2.5/Hg in coal-fired smoke |
| CN107029501B (en) * | 2016-12-19 | 2019-10-08 | 湖南顶立科技有限公司 | A kind of calcining exhaust gas processing device |
| CN106693594A (en) * | 2016-12-29 | 2017-05-24 | 龙伍洋 | Waste gas treatment method and system |
| CN106823722A (en) * | 2017-03-10 | 2017-06-13 | 东南大学 | A kind of apparatus and method of thermal activation oxidant combined steam synergistic purification flue gas |
| CN106823723A (en) * | 2017-03-10 | 2017-06-13 | 东南大学 | A kind of photoelectric induction free radical combined steam phase transformation smoke eliminator and method |
| CN108057335A (en) * | 2017-11-15 | 2018-05-22 | 广汉市航佳食品有限公司 | A kind of animal fat processing exhaust treatment system and its technique |
| CN107952365B (en) * | 2017-12-01 | 2024-05-10 | 中国电建集团河北省电力勘测设计研究院有限公司 | High-temperature flue gas evaporation desulfurization wastewater treatment device and treatment method thereof |
| CN108434960A (en) * | 2018-03-23 | 2018-08-24 | 东南大学 | A kind of devices and methods therefor promoting double tower Two-way Cycle wet desulfurization system removing fine particle and sulfur trioxide acid mist |
| CN109173552A (en) * | 2018-10-15 | 2019-01-11 | 中石化（洛阳）科技有限公司 | A kind of flue gas purifying method and system |
| CN110180295B (en) * | 2019-07-05 | 2023-06-27 | 郑州机械研究所有限公司 | Smoke purification method and device thereof |
| CN110624340A (en) * | 2019-09-18 | 2019-12-31 | 东南大学 | Dust removal pretreatment device and method based on water vapor charge phase change |
| CN110749481A (en) * | 2019-11-18 | 2020-02-04 | 国电环境保护研究院有限公司 | Sampling device and sampling method for low-concentration total particulate matters in flue gas of thermal power plant |
-
2007
- 2007-10-26 CN CN200710133987A patent/CN100594051C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN101224367A (en) | 2008-07-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100594051C (en) | Method of removing PM2.5 and gaseous pollutant using steam phase transition and device thereof | |
| CN101219333A (en) | Method and device for cooperation-removal of PM2,5 in flue gas wet desulphurization | |
| Shuangchen et al. | Environmental influence and countermeasures for high humidity flue gas discharging from power plants | |
| Wu et al. | Improving the removal of fine particles by heterogeneous condensation during WFGD processes | |
| AU2010325773B2 (en) | A method and device for cleaning a carbon dioxide rich flue gas | |
| CN109045953A (en) | A kind of cooling dehumidification by condensation decontamination reheating of flue gas disappears white system and method | |
| CN101732977B (en) | Device and method for improving fine particle removal in coal-fired flue gas desulfurization process | |
| WO2016058141A1 (en) | Method and device for dedusting and desulphurizing flue gas | |
| CN201105202Y (en) | Device for synergetic removing fine grains in flue gas wet desulfurization | |
| CN102059029A (en) | Method and device for removing fine particles in high-humidity gas fume | |
| CN103868087A (en) | Method and device for cooperatively enhancing PM2.5 (Particulate Matter 2.5) removal and smoke afterheat deep utilization | |
| CN208008493U (en) | A kind of equipment that flue residue heat is used for Waste Water From Fire Power Plant zero discharge treatment | |
| CN106669345A (en) | Method for synergistically realizing efficient removal of PM2.5/SO3 in high-moisture flue gas and zero water consumption in wet desulphurization | |
| CN206823458U (en) | A kind of coal-burning power plant's energy-saving dedusting synergy cooperative intelligentization regulation and control remove white system | |
| CN106621680A (en) | Method and system for deeply removing dust from flue gas after wet desulfurization | |
| CN101732970A (en) | Device and method for promoting fine particle matters to be removed in coal-burning wet flue gas desulfuration process | |
| CN107008098A (en) | Eliminate the device and removing method of fuel boiler flue gas hangover | |
| CN107777820A (en) | The technique that Air-Cooling Island exhaust steam residual heat is used for Waste Water From Fire Power Plant zero discharge treatment | |
| CN206799197U (en) | A kind of undersaturation flue gas condensing crystallizing desulfurization wastewater zero-discharge treatment system | |
| CN106348373A (en) | Wastewater evaporation equipment and wastewater treatment method and device | |
| CN111569630B (en) | Wet desulfurization system and wet desulfurization method | |
| CN107158913A (en) | A kind of apparatus and method of the ultra-clean dedusting of desulfurization fume | |
| CN205340465U (en) | High -efficient msw incineration schizolysis gas cleaning system | |
| CN201880450U (en) | Device for removing fine particulate matter from high-humidity flue gas | |
| CN107725194B (en) | Collection pollutant cleaning filtering is cooled in integrated gas turbine inlet air processing system with evaporation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100317 Termination date: 20161026 |