CN103721548A - Desulfurization device and desulfurization method for promoting removal of PM2.5 in clean flue gas after wet desulphurization - Google Patents

Desulfurization device and desulfurization method for promoting removal of PM2.5 in clean flue gas after wet desulphurization Download PDF

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CN103721548A
CN103721548A CN201410022770.6A CN201410022770A CN103721548A CN 103721548 A CN103721548 A CN 103721548A CN 201410022770 A CN201410022770 A CN 201410022770A CN 103721548 A CN103721548 A CN 103721548A
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flue gas
desulfurization
humid air
desulphurization
cleaning solution
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CN201410022770.6A
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CN103721548B (en
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杨林军
潘丹萍
吴昊
姜业正
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东南大学
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Abstract

The invention discloses a desulphurization device and a desulphurization method for promoting removal of PM2.5 in clean flue gas after wet desulphurization. The desulphurization device comprises a flue gas desulphurization washing device and a fog drop collecting device which are connected in series, wherein the flue gas desulphurization washing device comprises a desulphurization liquid oxidation region, a desulphurization washing region and a water vapor phase change region which are arranged in sequence from bottom to top; the fog drop collecting device forms an integral or split structure together with the flue gas desulphurization washing device and is arranged on the flue gas desulphurization washing device or at an outlet. According to the method, flue gas enters the water vapor phase change region after SO2 is removed through the desulphurization washing region; wet air is filled through a wet air distributor, so that the clean flue gas after the wet desulphurization reaches an oversaturated state; oversaturated water vapor is nucleated and condensed on the PM2.5 surface, so that the PM2.5 is turned into dust fog drops with liquid films on the surfaces and the particle sizes are increased; the condensed expanded dust fog drops enter the fog drop collecting device and are collected through fog drop washing liquid and a defroster of the fog drop collecting device. According to the desulphurization device, the energy consumption for building an oversaturated water vapor environment can be effectively reduced and the PM2.5 emission problem of a wet flue gas desulphurization system is solved.

Description

PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the desulfurizer removing and method thereof

Technical field

The invention belongs to PM in a kind of flue gas 2.5the technical field of emission control, particularly a kind of application steam Transformation Principle promotes PM in the clean flue gas of wet desulphurization 2.5the desulfurizer removing and method thereof.

Background technology

Wet process of FGD (WFGD) has become China and has removed SO 2mainstream technology, more than 80% big-and-middle-sized coal fired power plant adopts wet fuel gas desulfurizing technology, this technique application in fields such as coal-burned industrial boiler, sinter fumes also increases increasingly.In WFGD process, due to the cleaning function of desulfurization slurry, though can remove the meal dirt in flue gas, owing to existing, desulfurization slurry atomization is carried secretly, desulfurization product crystallization, and the materializing procedure such as various solution-airs, gas-liquid-solid desulphurization reaction, itself may form PM again 2.5, make flue gas PM after wet desulphurization 2.5concentration of emission increases on the contrary.As the coal-burning power plant of WFGD system is installed, and enter the fine particle of atmospheric environment except burned-coal fly ash, also comprise the inorganic salts particulate that sulfuric acid mist, desulfurization form; Holland Meij analyzes and finds, limestone/gypsum method desulphurization system outlet fine particle belongs to PM substantially 2.5, except burned-coal fly ash, also containing component (Fuel Processing Technology, 2004,85 (6-7): 641-656) such as gypsum and unreacted lime stones.

Adopt the dust removal installations such as electricity bag, cloth bag, Novel electric dedusting can only reduce the PM that enters wet desulfuration tower 2.5concentration, for the PM forming in WFGD process 2.5helpless; Though wet-esp is installed in WFGD system downstream, can effectively remove the PM in the clean flue gas of desulfurization 2.5, but because investment operating cost is higher, be also difficult to enter the comprehensive practical stage.In addition, in view of after smoke-gas wet desulfurization in saturation state, based on supersaturated vapor the steam phase change technique of microparticle surfaces congealing property be promote the clean flue gas of wet desulphurization in PM 2.5the important measures that remove, adopt this technology first will make the clean flue gas of wet desulphurization reach supersaturation, and the most simple measure is to add steam or heat exchanger is set to make flue gas cooling, but the latter can cause supersaturated vapor to be mainly condensed in heat exchanger wall, weakens PM 2.5condensation growth effect, and energy consumption is higher.Adopt the degree of supersaturation that interpolation steam mode is set up to raise and sharply reduce with the clean flue-gas temperature of desulfurization, while making to be applied to the occasion of the clean flue-gas temperature of desulfurization higher (>=55~70 ℃), steam consumption quantity is too high.Application number is that 200710132250.0 patent of invention discloses a kind of employing and in the clean flue gas of desulfurization, adds steam and set up PM 2.5the supersaturated vapor environment that condensation growth is required, is then removed the method for the dust-laden droplet of condensation growth by mesh mist eliminator; But depend merely on interpolation steam mode and realize supersaturation, energy consumption is too high, particularly when the clean flue-gas temperature of desulfurization is higher.Meanwhile, in view of PM 2.5after condensation growth, become the dust-laden droplet that outer surface covers one deck liquid film, need be supporting with the cleaner that can remove droplet, as wet scrubber, demister etc., though wherein the dust-laden droplet of mesh mist eliminator after for condensation growth has preferably removal effect, but while being applied to desulfurization method of limestone-gypsum technique, easily stifled, and resistance is larger; Though deflection plate demister is current the most conventional wet desulfurization demister, its droplet to tens of microns just has better removal effect, and PM 2.5be difficult to condensation growth to this particle size range.

Summary of the invention

Goal of the invention: the present invention is directed to flue gas moisture content feature in saturation state after wet desulphurization, provide a kind of application steam Transformation Principle to promote PM in the clean flue gas of wet desulphurization 2.5the desulfurizer removing and method thereof.

Technical scheme: PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the desulfurizer removing, described desulfurizer is that a flue gas desulfurization wash mill and a fog drip gathering device are composed in series, described flue gas desulfurization wash mill is followed successively by doctor solution zoneofoxidation, desulfurization scrubbing section, steam phase change zone from bottom to top; In doctor solution zoneofoxidation, be provided with oxidation air import, supplement desulfurizing agent import and the outlet of desulfurization cleaning solution; At desulfurization scrubbing section, be disposed with from lower to upper smoke inlet, the import of desulfurization cleaning solution, mist separator of desulfurization and mist separator of desulfurization rinse water arrangement; Middle part, steam phase change zone is provided with humid air distributor; Described fog drip gathering device and flue gas desulfurization wash mill are integral type structure, be arranged on flue gas desulfurization wash mill, described fog drip gathering device is provided with cleaning solution collector, cleaning solution overfall, the import of droplet cleaning solution, fog drip gathering device demister and droplet mist eliminator flushing water device and exhanst gas outlet from bottom to top successively, and cleaning solution overfall is connected with mist separator of desulfurization rinse water arrangement and doctor solution zoneofoxidation by overflow pipe.

Described steam phase change zone size need meet the flue gas time of staying therein and be more than or equal to steam at PM 2.5surface coring condensation growth required time.

Described fog drip gathering device and flue gas desulfurization wash mill replace with split-type structural, described fog drip gathering device is provided with gas approach from lower to upper successively, the outlet of droplet cleaning solution, the import of droplet cleaning solution, fog drip gathering device demister and droplet mist eliminator flushing water device and exhanst gas outlet.

Described fog drip gathering device also installs 1~2 laminate ripple or ripple silk net structured packing additional, and packing specific area is 125~375m 2/ m 3, every layer of filler loading height is 500~1000mm.

Described humid air distributor is to consist of humid air supervisor, arm and bracing frame, in the sector region of 90~120 ° of same supervisor or tube sections, at least 3 qi-emitting holes are evenly set, qi-emitting hole is 200~500mm along humid air supervisor or the axial pitch of holes of arm, and the aperture of qi-emitting hole is 3~10mm.

A kind of application promotes PM in the clean flue gas of wet desulphurization 2.5the sulfur method of the desulfurizer removing, is characterized in that, removes step to be: flue gas by desulfurization scrubbing section bottom enter after and desulfurization cleaning solution counter current contacting, after desulfurization scrubbing section by water-vapo(u)r saturation or approach saturated, cigarette temperature drop to 55~70 ℃; Then after removing desulfurization slurry droplet by mist separator of desulfurization, enter steam phase change zone, through humid air distributor, inject humid air, caloic exchange occurs between the clean flue gas of humid air and desulfurization, make the clean flue gas of desulfurization reach hypersaturated state, supersaturated vapor is at PM 2.5there is coring and condense in surface, makes PM 2.5become the dust-laden droplet of surface coverage one deck liquid film, particle diameter increases, the dust-laden droplet of condensation growth enters fog drip gathering device, by the droplet cleaning solution spraying into, remove the dust-laden droplet of condensation growth, then by the flue gas after fog drip gathering device demister trapping cleaning solution droplet, by exhanst gas outlet, discharged.

Described humid air addition is 10~25% of the clean flue gas volume amount of desulfurization, humid air temperature is lower more than 20 ℃ than the clean flue gas of desulfurization, humid air relative humidity RH >=60%, increases to S=1.05~1.20 so that the clean flue gas of desulfurization mixes rear flue gas degree of supersaturation S with humid air by S ≈ 1.00.

Described humid air is taken from coal fired power plant cooling tower through T≤40 with the exchange of recirculated cooling water generation caloic ℃, the humid air of RH >=85%, or T≤35 after work of water sprinkling for better material moisture ℃, RH >=80% humid air, or directly take from T≤25 in atmospheric environment ℃, RH >=60% Low Temperature Wet air.

Liquid-gas ratio in fog drip gathering device is controlled at 1~5L/Nm 3; Cleaning solution and mist eliminator flushing water after trapping dust-laden droplet are collected and are partly come together in doctor solution zoneofoxidation by overflow pipe by cleaning solution collector, and part is as the flushing water of mist separator of desulfurization.

Beneficial effect:

1. utilizing supersaturated vapor is to impel PM at the coring congealing property of microparticle surfaces 2.5the important measures that granularity increases, are particularly suitable for the higher process of moisture content in flue gas; Flue gas is after wet desulphurization, and flue gas relative humidity increases and the state that can approach or reach capacity, and more easily sets up PM 2.5the supersaturated vapor environment that condensation growth is required.

2. the non-linear relation based between humid gas saturated vapor pressure and temperature, mix the gas of two bursts of different humitures and can set up supersaturated vapor environment, the clean flue gas of its principle and wet desulphurization enters that to produce in white mist and atmospheric environment warm moist air and the cold air formation precipitation that crosses after atmospheric environment similar.The present invention utilizes above-mentioned know-why, by the clean flue gas of desulfurization, introduce temperature than desulfurization the low more than 20 ℃ humid air of clean flue gas set up PM 2.5the supersaturated condition that condensation growth is required, and the degree of supersaturation of mist raises and increases with the clean flue-gas temperature of desulfurization, is particularly suitable for the occasion of the clean flue-gas temperature of desulfurization higher (>=55~70 ℃); Flue gas cooling provision is compared with adding steam or heat exchanger is set, can significantly be reduced and set up PM 2.5the energy consumption of the required supersaturated vapor environment of condensation growth.

3. the present invention is by arranging fog drip gathering device at flue gas desulfurization wash mill top or outlet, by the dust-laden droplet after droplet cleaning solution and fog drip gathering device demister trapping condensation growth, and promote washing trapping effect by installing 1~2 laminate ripple or ripple silk net structured packing additional.On the one hand, arresting efficiency significantly improves; Meanwhile, because the dust-laden droplet of condensation growth is washed trapping before entering fog drip gathering device demister substantially, can effectively solve and depend merely on demister trapping, the susceptible to plugging defect of demister in running.

4. technique of the present invention is simple, as long as desulfurizer is simply transformed, steam phase change zone is set in flue gas desulfurization wash mill, and top or outlet arrange fog drip gathering device, and humid air distributor is installed in steam phase change zone, introduces appropriate humid air; Can guarantee, under the prerequisite of desulfuration efficiency, effectively to remove the PM forming in based Wet Process Flue Gas 2.5(as gypsum, SO 3acid mist etc.), can be widely used in being provided with the coal fired power plant, coal-burned industrial boiler, sintering plant etc. of WFGD system.With in WFGD system downstream, wet electrical dust precipitator is installed and is compared, investment operating cost is low.

Accompanying drawing explanation

Fig. 1 is the apparatus structure schematic diagram of the embodiment of the present invention 1;

Fig. 2 is the apparatus structure schematic diagram of the embodiment of the present invention 2;

Fig. 3 is humid air structure of distributor schematic diagram of the present invention.

In figure: 1-desulfurizing tower; 2-doctor solution nozzle; 3-mist separator of desulfurization; 4-humid air distributor; 4-1-humid air supervisor, 4-2-arm; 4-3-bracing frame; 5-cleaning solution feeder; 6-fog drip gathering device filler; 7-fog drip gathering device demister; 8-overflow pipe; 9-doctor solution circulating pump; 10-droplet detergent circulator; A-doctor solution zoneofoxidation; B-desulfurization scrubbing section; C-steam phase change zone; D-fog drip gathering device.

The specific embodiment

Below in conjunction with Fig. 1~3, the present invention is elaborated:

PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the desulfurizer removing, is that a flue gas desulfurization wash mill and a fog drip gathering device are composed in series, and described flue gas desulfurization wash mill and fog drip gathering device can be also split type setting for integral type.When being integral type, integral body is desulfurizing tower form, and described flue gas desulfurization wash mill is followed successively by doctor solution zoneofoxidation, desulfurization scrubbing section, steam phase change zone from bottom to top; In doctor solution zoneofoxidation, be provided with oxidation air import, supplement desulfurizing agent import and the outlet of desulfurization cleaning solution; At desulfurization scrubbing section, be disposed with from lower to upper smoke inlet, the import of desulfurization cleaning solution, mist separator of desulfurization and mist separator of desulfurization rinse water arrangement; Middle part, steam phase change zone is provided with humid air distributor; Described fog drip gathering device and flue gas desulfurization wash mill are integral type structure, be arranged on flue gas desulfurization wash mill, described fog drip gathering device is provided with cleaning solution collector, cleaning solution overfall, the import of droplet cleaning solution, fog drip gathering device demister and droplet mist eliminator flushing water device and exhanst gas outlet from bottom to top successively, and cleaning solution overfall is connected with mist separator of desulfurization rinse water arrangement and doctor solution zoneofoxidation by overflow pipe.

PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the desulfurizer removing, the size of the steam phase change zone in described desulfurizer is no less than steam at PM with the flue gas time of staying therein 2.5surface coring condensation growth required time is definite, approximately 50~200ms.Described fog drip gathering device can install 1~2 laminate ripple or ripple silk net structured packing additional, and packing specific area is 125~375m 2/ m 3, every layer of filler loading height is 500~1000mm.PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the desulfurizer removing, described fog drip gathering device and the split type layout of flue gas desulfurization wash mill.

Described fog drip gathering device can be spray scrubber, stuffing washing tower; When being split-type structural, except first two can also be selected Venturi scrubber structure.

Described droplet cleaning solution outlet is connected with the import of droplet cleaning solution by droplet detergent circulator.

PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the desulfurizer removing, described humid air distributor is to consist of humid air supervisor and arm, in same supervisor or 90~120 ° of sector regions of tube section, 3 qi-emitting holes are evenly set, axial hole spacing is 200~500mm, and the aperture of qi-emitting hole is 3~10mm.

The desulfurization cleaning solution outlet of doctor solution zoneofoxidation is connected with the desulfurization cleaning solution import of doctor solution scrubbing section by doctor solution circulating pump.

PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the method removing, it removes step and is: flue gas after the desulfurization scrubbing section of desulfurizing tower by water-vapo(u)r saturation or approach saturated, cigarette temperature drop to 55~70 ℃; Then after removing water smoke by mist separator of desulfurization, enter steam phase change zone, through humid air distributor, inject appropriate humid air, caloic exchange occurs between the clean flue gas of humid air and desulfurization, make the clean flue gas of desulfurization reach hypersaturated state, supersaturated vapor is at PM 2.5there is coring and condense in surface, makes PM 2.5become the dust-laden droplet of surface coverage one deck liquid film, particle diameter increases, and the dust-laden droplet of condensation growth enters fog drip gathering device, by cleaning solution and the demister of being located at fog drip gathering device top, is trapped.

PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the method removing, described humid air addition is 10~25% of the clean flue gas volume amount of desulfurization, humid air temperature is lower more than 20 ℃ than the clean flue gas of desulfurization, and humid air relative humidity RH>=60% increases to S=1.05~1.20 so that the clean flue gas of desulfurization mixes rear flue gas degree of supersaturation S with humid air by S ≈ 1.00.

PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the method removing, in the desirable spontaneous combustion coal Cooling Tower of Power Station of described humid air through humid air (T≤40 ℃ with recirculated cooling water generation caloic exchange; RH>=85%), humid air (T≤35 ℃ or after work of water sprinkling for better material moisture; RH>=80%), also can directly take from Low Temperature Wet air (T≤25 ℃ in atmospheric environment; RH>=60%).

PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the method removing, described fog drip gathering device liquid-gas ratio 1~5L/Nm 3; Cleaning solution and mist eliminator flushing water after trapping dust-laden droplet are collected and are partly come together in doctor solution zoneofoxidation by overflow pipe by cleaning solution collector, and part is as the flushing water of mist separator of desulfurization.

Embodiment 1:

A desulfurizer, is applied to PM in the described clean flue gas of promotion wet desulphurization 2.5in the method removing, the desulfurizing tower 1 of described desulfurizer is an absorption tower with multistage functional section, and tower bottom is doctor solution zoneofoxidation A, and middle part is desulfurization scrubbing section B, and top is PM 2.5the fog drip gathering device D of dust-laden droplet after the steam phase change zone C of condensation growth occurring and trapping condensation growth.At doctor solution zoneofoxidation A, be provided with oxidation air import, supplement desulfurizing agent import and the outlet of desulfurization cleaning solution.Bottom at desulfurization scrubbing section B is provided with gas approach, and top is provided with the import of desulfurization cleaning solution, can adopt hollow-spraying-tower, column plate or filling-material structure.C middle part in steam phase change zone is provided with humid air distributor 4, humid air distributor 4 is to consist of humid air supervisor 4-1, arm 4-2 and bracing frame 4-3, in same supervisor or 90~120 ° of sector regions of tube section, 3 qi-emitting holes are evenly set, axial hole spacing is 200~500mm, and the aperture of qi-emitting hole is 3~10mm; The size of steam phase change zone C is no less than steam at PM with the flue gas time of staying therein 2.5surface coring condensation growth required time is definite, approximately 50~200ms.Fog drip gathering device D can install 1~2 laminate ripple additional or ripple silk net structured packing forms droplet trapping district filler 6, and the specific area of droplet trapping district filler 6 is 125~375m 2/ m 3, every layer of filler loading height is 500~1000mm.Between desulfurization scrubbing section B and steam phase change zone C, be provided with mist separator of desulfurization 3 and mist eliminator flushing water system; Between steam phase change zone C and fog drip gathering device D, be provided with cleaning solution collector 5; Cleaning solution collector 5 communicates with mist separator of desulfurization rinse water arrangement and doctor solution zoneofoxidation A by overflow pipe 8; Fog drip gathering device D top is provided with fog drip gathering device demister 7 and mist eliminator flushing water device.Mist separator of desulfurization 3 is selected lower resistance demister, and as deflection plate demister, rotational flow plate defroster, fog drip gathering device demister 7 is selected efficient demister, as Lamb wave line demister, mesh mist eliminator.

According to the present invention, PM in the clean flue gas of a kind of promotion wet desulphurization 2.5the method removing is as shown in Figure 1: flue gas is entered in tower by desulfurizing tower 1 bottom smoke inlet, with the desulfurization cleaning solution counter current contacting through circulating pump 9,2 ejections of doctor solution nozzle, flue gas with doctor solution counter current contacting process in be humidified cooling, after desulfurization scrubbing section B by water-vapo(u)r saturation or approach saturated, cigarette temperature drop to 55~70 ℃.Then after removing desulfurization slurry droplet by mist separator of desulfurization 3, enter steam phase change zone C, through humid air distributor 4, inject appropriate humid air, caloic exchange occurs between the clean flue gas of humid air and desulfurization, make the clean flue gas of desulfurization reach hypersaturated state, supersaturated vapor is at PM 2.5there is coring and condense in surface, makes PM 2.5become the dust-laden droplet of surface coverage one deck liquid film, particle diameter increases, mass penalty; Humid air addition is 10~25% of the clean flue gas volume amount of desulfurization, humid air temperature is lower more than 20 ℃ than the clean flue gas of desulfurization, humid air relative humidity RH>=60%, increases to S=1.05~1.20 so that the clean flue gas of desulfurization mixes rear flue gas degree of supersaturation S with humid air by S ≈ 1.00; In the desirable spontaneous combustion coal Cooling Tower of Power Station of humid air through humid air (T≤40 ℃ with recirculated cooling water generation caloic exchange; RH>=85%), humid air (T≤35 ℃ or after work of water sprinkling for better material moisture; RH>=80%), also can directly take from Low Temperature Wet air (T≤25 ℃ in atmospheric environment; RH>=60%).The dust-laden droplet of condensation growth enters fog drip gathering device D, and by the droplet cleaning solution that sprays into, to remove the dust-laden droplet of condensation growth, the liquid-gas ratio of controlling in fog drip gathering device is 1~5L/Nm 3, then after fog drip gathering device demister 7 trapping cleaning solution droplets by the exhanst gas outlet at desulfurizing tower 1 top through smoke stack emission.Cleaning solution after trapping dust-laden droplet and mist eliminator flushing water are collected and are come together in doctor solution zoneofoxidation A by overflow pipe 8 parts by cleaning solution collector 5, and part is as the flushing water of mist separator of desulfurization 3.

Embodiment 2:

As shown in Figure 2, as different from Example 1, fog drip gathering device D and flue gas desulfurization wash mill are split type setting, and flue gas desulfurization wash mill is desulfurizing tower 1, and 1 of desulfurizing tower comprises doctor solution zoneofoxidation A, desulfurization scrubbing section B and steam phase change zone C; Described fog drip gathering device can be the structures such as spray scrubber, stuffing washing tower, Venturi scrubber, cleaning solution and mist eliminator flushing water section after trapping dust-laden droplet recycle through droplet detergent circulator 10, and part is returned to doctor solution zoneofoxidation A or as the flushing water of mist separator of desulfurization 3.All the other are with embodiment 1.

Embodiment 3:

Flue gas is produced by fully-automatic coal-fired boiler, and exhaust gas volumn is 300Nm 3/ h, desulfurizing tower adopts the spray column of tower diameter 200mm, tower height 4500mm, three grades of sprays, liquid-gas ratio 18L/Nm 3, Wet Flue Gas Desulfurization Technique is limestone-gypsum method.Desulfurizing tower top arranges steam phase change zone and fog drip gathering device, between steam phase change zone and desulfurization scrubbing section, deflection plate demister is installed; Between steam phase change zone and fog drip gathering device, be provided with cleaning solution collector, cleaning solution collector communicates with doctor solution zoneofoxidation by overflow pipe, and middle part, steam phase change zone is provided with humid air distributor; Droplet trapping is installed two metal perforated plate corrugated regular fillers in district, and packing specific area is 250m 2/ m 3, packing layer height overall 500mm; DP type (heavy duty detergent) mesh mist eliminator is installed in fog drip gathering device outlet, the high 150mm of demister, and demister is specific area 625m 2/ m 3.The ash-laden gas that fully-automatic coal-fired boiler produces enters the desulfurization scrubbing section of desulfurizing tower after electric cleaner removes meal dirt, with limestone desulfurization slurries counter current contacting; Flue gas removes SO through desulfurization scrubbing section 2after enter successively steam phase transformation chamber, fog drip gathering device.Through the parallel full-automatic flue dust sampling instrument test of WJ-60B type Pitot tube, desulfurizing tower outlet dust total concentration is 42mg/m 3; Wherein, adopt Electrical low pressure impactor ELPI on-line testing, desulfurizing tower outlet PM 2.5mass concentration is 16mg/m 3.By humid air distributor at the every Nm in steam phase change zone 3in flue gas, inject 0.15Nm 3humid air, 18 ℃ of humid air temperature (lower 45 ℃ than the clean flue gas of desulfurization), humid air relative humidity is 70%, droplet scrubbing section spray 0.6m 3/ h washings (liquid-gas ratio 2L/Nm 3); After tested, desulfurizing tower outlet dust total concentration, PM 2.5mass concentration is down to respectively 18mg/m 3, 8mg/m 3.

Claims (9)

1. one kind promotes PM in the clean flue gas of wet desulphurization 2.5the desulfurizer removing, it is characterized in that, described desulfurizer is that a flue gas desulfurization wash mill and a fog drip gathering device are composed in series, and described flue gas desulfurization wash mill is followed successively by doctor solution zoneofoxidation, desulfurization scrubbing section, steam phase change zone from bottom to top; In doctor solution zoneofoxidation, be provided with oxidation air import, supplement desulfurizing agent import and the outlet of desulfurization cleaning solution; At desulfurization scrubbing section, be disposed with from lower to upper smoke inlet, the import of desulfurization cleaning solution, mist separator of desulfurization and mist separator of desulfurization rinse water arrangement; Middle part, steam phase change zone is provided with humid air distributor; Described fog drip gathering device and flue gas desulfurization wash mill are integral type structure, be arranged on flue gas desulfurization wash mill, described fog drip gathering device is provided with cleaning solution collector, cleaning solution overfall, the import of droplet cleaning solution, fog drip gathering device demister and droplet mist eliminator flushing water device and exhanst gas outlet from bottom to top successively, and cleaning solution overfall is connected with mist separator of desulfurization rinse water arrangement and doctor solution zoneofoxidation by overflow pipe.
2. PM in the clean flue gas of promotion wet desulphurization according to claim 1 2.5the desulfurizer removing, is characterized in that, described steam phase change zone size need meet the flue gas time of staying therein and be more than or equal to steam at PM 2.5surface coring condensation growth required time.
3. PM in the clean flue gas of promotion wet desulphurization according to claim 1 2.5the desulfurizer removing, it is characterized in that, described fog drip gathering device and flue gas desulfurization wash mill replace with split-type structural, described fog drip gathering device is provided with gas approach from lower to upper successively, the outlet of droplet cleaning solution, the import of droplet cleaning solution, fog drip gathering device demister and droplet mist eliminator flushing water device and exhanst gas outlet.
4. according to PM in the clean flue gas of promotion wet desulphurization described in claim 1 or 3 2.5the desulfurizer removing, is characterized in that, described fog drip gathering device also installs 1~2 laminate ripple or ripple silk net structured packing additional, and packing specific area is 125~375m 2/ m 3, every layer of filler loading height is 500~1000mm.
5. according to PM in the clean flue gas of promotion wet desulphurization described in claim 1 or 3 2.5the desulfurizer removing, it is characterized in that, described humid air distributor is to consist of humid air supervisor, arm and bracing frame, in the sector region of 90~120 ° of same supervisor or tube sections, at least 3 qi-emitting holes are evenly set, qi-emitting hole is 200~500mm along humid air supervisor or the axial pitch of holes of arm, and the aperture of qi-emitting hole is 3~10mm.
6. an application rights requires PM in the clean flue gas of 1~5 arbitrary promotion wet desulphurization 2.5the sulfur method of the desulfurizer removing, is characterized in that, removes step to be: flue gas by desulfurization scrubbing section bottom enter after and desulfurization cleaning solution counter current contacting, after desulfurization scrubbing section by water-vapo(u)r saturation or approach saturated, cigarette temperature drop to 55~70 ℃; Then after removing desulfurization slurry droplet by mist separator of desulfurization, enter steam phase change zone, through humid air distributor, inject humid air, caloic exchange occurs between the clean flue gas of humid air and desulfurization, make the clean flue gas of desulfurization reach hypersaturated state, supersaturated vapor is at PM 2.5there is coring and condense in surface, makes PM 2.5become the dust-laden droplet of surface coverage one deck liquid film, particle diameter increases, the dust-laden droplet of condensation growth enters fog drip gathering device, by the droplet cleaning solution spraying into, remove the dust-laden droplet of condensation growth, then by the flue gas after fog drip gathering device demister trapping cleaning solution droplet, by exhanst gas outlet, discharged.
7. application according to claim 8 promotes PM in the clean flue gas of wet desulphurization 2.5the sulfur method of the desulfurizer removing, it is characterized in that, described humid air addition is 10~25% of the clean flue gas volume amount of desulfurization, humid air temperature is lower more than 20 ℃ than the clean flue gas of desulfurization, humid air relative humidity RH>=60%, increases to S=1.05~1.20 so that the clean flue gas of desulfurization mixes rear flue gas degree of supersaturation S with humid air by S ≈ 1.00.
8. application according to claim 7 promotes PM in the clean flue gas of wet desulphurization 2.5the sulfur method of the desulfurizer removing, it is characterized in that, described humid air is taken from coal fired power plant cooling tower through T≤40 with the exchange of recirculated cooling water generation caloic ℃, the humid air of RH>=85%, or T≤35 after work of water sprinkling for better material moisture ℃, RH>=80% humid air, or directly take from T≤25 in atmospheric environment ℃, RH>=60% Low Temperature Wet air.
9. application according to claim 7 promotes PM in the clean flue gas of wet desulphurization 2.5the sulfur method of the desulfurizer removing, is characterized in that, the liquid-gas ratio in fog drip gathering device is controlled at 1~5L/Nm 3; Cleaning solution and mist eliminator flushing water after trapping dust-laden droplet are collected and are partly come together in doctor solution zoneofoxidation by overflow pipe by cleaning solution collector, and part is as the flushing water of mist separator of desulfurization.
CN201410022770.6A 2014-01-17 2014-01-17 PM in a kind of promotion wet desulphurization neat stress 2.5the desulfurizer removed and method thereof CN103721548B (en)

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