CN108619884A - Fume desulfurizing tower and flue gas ash removal, desulfurization and wastewater treatment method - Google Patents

Fume desulfurizing tower and flue gas ash removal, desulfurization and wastewater treatment method Download PDF

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Publication number
CN108619884A
CN108619884A CN201710182033.6A CN201710182033A CN108619884A CN 108619884 A CN108619884 A CN 108619884A CN 201710182033 A CN201710182033 A CN 201710182033A CN 108619884 A CN108619884 A CN 108619884A
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China
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flue gas
area
zone
oxidizing
pipeline
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CN201710182033.6A
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CN108619884B (en
Inventor
李磊
李欣
齐慧敏
刘忠生
杨秀娜
王昊辰
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Sinopec Dalian Petrochemical Research Institute Co ltd
China Petroleum and Chemical Corp
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China Petroleum and Chemical Corp
Sinopec Dalian Research Institute of Petroleum and Petrochemicals
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/06—Spray cleaning
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • B01D50/40—Combinations of devices covered by groups B01D45/00 and B01D47/00
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/80—Semi-solid phase processes, i.e. by using slurries
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides

Abstract

The invention discloses a kind of fume desulfurizing tower and flue gas ash removal, desulfurization and wastewater treatment methods.A kind of fume desulfurizing tower is from top to bottom followed successively by flue gas emission area, mist eliminating zone, tower tray area, spraying zone and wastewater treatment area；The wastewater treatment area is oxidizing, flocculating area and circulation cleaning liquid zone by one piece of I points of vertical clapboard, and circulation cleaning liquid zone top is completely separated by circulation cleaning liquid zone and oxidizing, flocculating area and spraying zone by partition board II；Filter medium is arranged in the vertical clapboard I；The flue gas pipeline II is extended to inside oxidizing, flocculating area, the horizontal distribution several groups flue gas branch pipes successively from down to up of the flue gas pipeline II inside oxidizing, flocculating area.The present invention carries out flue gas ash removal, desulfurization and wastewater treatment in a tower, and floor space is greatly reduced, and reduces expense and device operating cost needed for plant construction, transformation.

Description

Fume desulfurizing tower and flue gas ash removal, desulfurization and wastewater treatment method
Technical field
The invention belongs to industrial waste gas purifying field, it is related at a kind of fume desulfurizing tower and flue gas ash removal, desulfurization and waste water Reason method.
Background technology
Contain sulfur dioxide and dust in the flue gas of boiler smoke and plant emissions, sulfur dioxide and dust are air dirts The main composition dust of object is contaminated, sulfur dioxide is the main reason for forming acid rain, and the smaller dust of grain size is the haze to be formed crime One of stalwart chief culprit.
Environmental pollution getting worse, haze event take place frequently, and country is also higher and higher to the attention degree of environmental protection, goes out in recent years A series of platform laws and regulations, national standard, the management method of environmental protections.GB 13223-2011 《Thermal power plant's atmosphere pollution Object discharge standard》Regulation：Fire coal boiler fume dust ≯ 30mg/Nm3, the SO of new construction of coal-fired boiler flue gas2≯100mg/Nm3；Weight The regional fire coal boiler fume dust ≯ 20mg/Nm of point3, SO2≯50mg/Nm3.《Implement in full coal-burning power plant's minimum discharge and section It can retrofit work scheme》（Ring sends out [2015] No. 164）Middle regulation coal-fired plant flue gas minimum discharge index is：Exhaust gas dust ≯ 10mg/Nm3, SO2≯25mg/Nm3.GB 31570-2015《Petroleum refining industry pollutant emission standard》Regulation：Catalytic cracking Catalyst regeneration flue gas particles ≯ 50mg/Nm3, SO2≯100mg/Nm3；Key area particulate matter ≯ 30mg/Nm3, SO2≯ 50mg/Nm3。
Wet desulphurization is high with desulfurization degree, device is reliable for operation, simple operation and other advantages, thus the existing cigarette in countries in the world Desulfurization technology is mainly based on wet desulphurization.Traditional Wet Flue Gas Desulfurization Technique mainly has limestone-gypsum method, Dual alkali de- Sulphur, sodium alkali desulfurization, ammonia process of desulfurization method etc..Above-mentioned flue gas desulfurization technique mainly uses countercurrent spray, and alkaline slurry is from desulfurizing tower Top is sprayed, and free settling is contacted with flue gas adverse current under the effect of gravity realizes desulphurization reaction, but the liquid due to spraying out It is relatively large to drip diameter, the contact area very little of single drop and flue gas needs to improve serum recycle to improve desulfuration efficiency The number of spray makes assimilation effect of the drop repeatedly with smoke contacts to improve drop to sulfur dioxide, thus bottom of tower slurries follow The flow of ring pump is very big, and power of motor is also very big, and the power consumption of slurry circulating pump is very big, and operating cost is higher.
The grain size of dust is smaller in flue gas, and most of between 0.1 ~ 200 μm, flue gas ash removal technology is mainly cloth bag at present Formula dedusting technology, electrostatic precipitator technology, wet dust collection technology.Due to containing moisture in flue gas, dust is in fiber bag precipitator Moisture absorption is cohered on filter bag, blocks the hole of filter bag, thus needs that frequently filter bag is cleared up or replaced, and fiber bag precipitator is answered With being extremely limited；The major defect of electrostatic precipitator is that cost is higher, and installation is safeguarded, manages requirement strictly, and height is needed Buckling electricity and commutation control equipment, power consumption is higher, and floor space is larger；Wet dust collection technology mainly removes cigarette by shower water After being combined with dust still chimney can be discharged with flue gas in the dust carried in gas, the smaller drop of grain size.
At desulfurization wastewater disclosed in CN201110153423.3, CN201310338193.7, CN201310421183.X Science and engineering skill is both provided with flocculation basin and oxidation tank, and flocculation basin and oxidation tank are both needed to setting blender, and slurries need to pass through machine Pump conveying.Dust-removal and desulfurizing waste water treatment process disclosed in CN201310338193.7, CN201310421183.X uses spinning liquid Separator is separated by solid-liquid separation.Above-mentioned FGD Wastewater Treatment Process is longer, and equipment is more, and energy consumption is also larger.
Since the disposal of pollutants index that country formulates is increasingly stringenter, possesses the enterprise of boiler and possess the work of flue gas emission Factory need to be to increasing flue-gas dust-removing and desulfurization device newly or being transformed to old device to meet flue gas qualified discharge.Due to most of boiler It is built according to pervious old plant with smoke discharging device, is not considered that flue gas needs further depth dedusting de- when building Sulphur, thus enough construction lands are not reserved to flue-gas dust-removing and desulfurization transformation when building, it is both needed in existing limited region Interior newly-built flue-gas dust-removing and desulfurization device is transformed old device.Above-mentioned Wet Flue Gas Desulfurization Technique is useless comprising flue gas desulfurization, desulfurization Water oxidation processes or regeneration unit, flow is longer, and equipment is more, and floor space is larger, seriously restricts dust-removing desulfurating apparatus Build and upgrading, partial devices and boiler in default of enough spaces can not upgrading, lead to flue gas emission index Existing national standards are cannot be satisfied to be forced to stop work or demolish to rebuild.Thus, it would be highly desirable to development process is short, equipment is few, floor space is few Flue gas desulfurization technique.
Invention content
In view of the deficiencies of the prior art, a kind of fume desulfurizing tower and flue gas ash removal of present invention offer, desulfurization and wastewater treatment Method, fume desulfurizing tower of the invention integrate flue gas ash removal, desulfurization and wastewater treatment, and the method for the present invention flow is short, equipment Less, floor space is few, has broad application prospects.
The fume desulfurizing tower of the present invention is from top to bottom followed successively by flue gas emission area, mist eliminating zone, tower tray area, spraying zone and gives up Water treatment zone；The wastewater treatment area center is oxidizing, flocculating area and circulation cleaning liquid zone by one piece vertical partition board I points, Middle oxidizing, flocculating area is connected to spraying zone, by partition board II by circulation cleaning liquid zone and oxidizing, flocculating area and spray at the top of circulation cleaning liquid zone It is completely separated to drench area；At least one opening, preferably 1 ~ 20, more preferably 1 ~ 4 is arranged in the partition board I, and opening area is The 10% ~ 90% of partition board I areas, preferably 50% ~ 70%；Filter medium is fixed in the opening of partition board I.
The filter medium is natural fiber, synthetic fibers, glass fiber, reticular structure made of wire, and mesh is big Small is 0.1 ~ 1000 μm, preferably 5 ~ 100 μm.
The both ends partition board II are connect with partition board I and circulation cleaning liquid zone tower wall respectively, partition board I and the junctions partition board II Angle is generally 45 ~ 165 °, preferably 120 ~ 150 °.It is sealed between the partition board I and partition board II and tower wall, avoids demarcation strip The air-liquid short circuit of both sides.
The flue gas emission area is preferably connected by cone-shaped reducing with mist eliminating zone, the mist eliminating zone and flue gas emission The tower diameter ratio in area is 1.2 ~ 5；Tower tray area is preferably connected by reverse taper deformation diameter with spraying zone, is wastewater treatment below spraying zone Area；The tower diameter ratio in the tower tray area and spraying zone is 1.2 ~ 3.
Exhanst gas outlet is set at the top of the flue gas emission area, the flue gas for discharging purification.
Defogging equipment is arranged in the mist eliminating zone, the drop for removing flue gas carrying, and the defogging equipment can be One or more of vortex-flow and defrosting device, wet-type electrostatic defroster, mesh mist eliminator or deflector type demister etc..
One or more layers tower tray can be arranged in the tower tray area, and the preferably tower tray number of plies is 2 ~ 6 layers；The tower tray can be one The tower tray or multiple types of type combine tower tray, including float valve tray, screen hole type tower tray, guiding screen hole type tower tray, Gu Sheta Disk, directional float tray or combined trapezoid spray tray etc. come into full contact with the deep desulfuration strengthened mass transfer and realize flue gas for gas-liquid, by flue gas In 0.1 μm ~ 5 μm between minute dusts particle capture get off to realize the depth dedusting of flue gas, and flue gas carried a large amount of Mist droplet captures the segregational load for reducing mist eliminating zone.
Liquid distribution trough is set between the tower tray area and mist eliminating zone, and liquid distribution trough connects circulating clear liquid pipeline I, uses It is evenly dispersed on tower tray in by circulating clear liquid.
The spraying zone top is arranged one or more layers spray pipe, when Multi-layer sprinkling pipeline is set, spray pipe it Between distance be 0.5 ~ 5m, preferred distance be 1 ~ 2.5m；The spray pipe connects circulating clear liquid pipeline II, on spray pipe It is provided with multiple atomizers；For circulating clear liquid to be atomized, the droplet after atomization connects the spraying zone with flue gas adverse current It touches, removes the dust and sulfur dioxide carried in flue gas；Smoke inlet I is arranged in the spraying zone lower part, for connecting flue gas Pipeline I.
The oxidizing, flocculating area is separately connected alkaline solution line I, flocculant line and liquid level gauge close to tower wall side I；Flow control valve is set on the alkaline solution line I, its pH value is adjusted for filling alkaline solution into desulfurization wastewater； The flocculant line makes the little particle dust cohesion in desulfurization wastewater at big for filling flocculant into desulfurization wastewater Grain.
The oxidizing, flocculating area bottom connection flue gas pipeline II and outer row's slurry line；The flue gas pipeline II extends To inside oxidizing, flocculating area and being parallel to partition board I, the horizontal distributions successively from down to up of the flue gas pipeline II inside oxidizing, flocculating area Several groups flue gas branch pipe, preferably 2 ~ 4 groups, flue gas branch pipe is connected to along gas pipeline II；Every group of flue gas branch pipe is by 2 ~ 8 cigarettes Gas branch pipe forms, and flue gas branch pipe is arc-shaped, and every group of flue gas branch pipe is uniformly distributed in the horizontal direction and rotation direction is identical；Flue gas from The direction that flue gas branch pipe sprays is the tangential direction of circular arc, and flue gas high speed, which sprays, pushes slurries rotation, for oxidizing, flocculating area Slurries be stirred, so that material in oxidizing, flocculating area is uniformly mixed, and dust particles on filter medium are rinsed；Institute The outer row's slurry line stated is used to drain into subsequent processing units outside the slurries after oxidizing, flocculating, and stream is arranged in outer row's slurry line Adjustable valve and pH meter；The flow of plasma discharge liquid outside the Signal Regulation that the flow control valve is fed back according to liquid level gauge I, for controlling The liquid level of system liquefaction flocculation zone；The pH meter is used to measure the pH value of outer plasma discharge liquid, and signal via controller is fed back to alkali Flow control valve on property solution pipeline I.
The circulation cleaning liquid zone is connected with fresh water pipeline, alkaline solution line II, oxidisability gas close to tower wall side Fluid line and liquid level gauge II；Flow control valve is set on the fresh water pipeline, according to the Signal Regulation of liquid level gauge II feedbacks The flow of fresh water is used for the liquid level of control loop clear liquid area；It is provided with flow control valve on the alkaline solution line II, Flow for adjusting the alkaline solution filled to circulation cleaning liquid zone；The oxidizing gas pipeline is connected with wind turbine, and prolongs The sides partition board I for reaching circulation cleaning liquid zone, are connected with oxidizing gas distributor pipe；It is arranged on the oxidizing gas distributor pipe There are several nozzles, nozzle to face the filter medium on partition board I, oxidizing gas sprays from nozzle and pass through filter medium, will Dust particles on oxidizing, flocculating area filter medium are blown afloat, and the slurries that the dust and oxidizing gas blown afloat is rotated are taken away, powder Dirt acts on coacervating large particle under the effect of gravity to oxidizing, flocculating area bottom deposit, into the oxygen in oxidizing, flocculating area with flocculant Sulfite oxidation in slurries is sulfate by the property changed gas, keeps the COD of desulfurization wastewater up to standard.
Blow vent is set on the circulation cleaning liquid zone top drum wall, for ensureing that circulation cleaning liquid zone pressure is steady, is avoided Pressure oscillation is excessive to damage filter medium.
The circulation cleaning liquid zone bottom connection clear liquid draws pipeline, draws pipeline and is divided into two-way, pipeline connection is outer all the way Liquid pipe line is cleared, another way pipeline connects circulation cleaning liquid pump, is provided with pH meter on the pipeline, circulation cleaning liquid pump is connected through cooler Circulating clear liquid pipeline I and circulating clear liquid pipeline II；The pH meter is used to measure the pH value of circulating clear liquid, and measuring signal is passed through Controller feeds back to the regulating valve of alkaline solution line II.
The flue gas ash removal of the present invention, the method for desulfurization and wastewater treatment, including following content：
（1）Flue gas divides two-way to enter fume desulfurizing tower, enters all the way from the spraying zone lower part of fume desulfurizing tower through flue gas pipeline I, Another way enters through the slurries in oxidizing, flocculating area through flue gas pipeline II from the oxidizing, flocculating area bottom of fume desulfurizing tower, and two Road flue gas converges the most of dust and sulfur dioxide carried in the circulating clear liquid counter current contacting removing flue gas with spraying zone afterwards, wears The flue gas for crossing spraying zone enters tower tray area, carries out depth dust-removal and desulfurizing in tower tray area and circulating clear liquid, purified flue gas passes through It is discharged from flue gas emission area after mist eliminating zone demisting；
（2）The desulfurization slurry for absorbing dust and sulfur dioxide enters oxidizing, flocculating area, in the flue gas entered through flue gas pipeline II Stirring action under be sufficiently mixed with oxidizing gas, flocculant and alkaline solution, the sulphite in desulfurization slurry is aoxidized For sulfate, the little particle dust in desulfurization slurry flocculates into bulky grain, while there is the flue gas of certain temperature to make desulfurization slurry In moisture constantly volatilize, salinity gradually increases；
（3）For desulfurization slurry under the action of partition board I both sides liquid level differences, the filter medium flowed through on partition board I realizes separation of solid and liquid, takes off Dust particles in sulphur slurries, which are filtered, stays in oxidizing, flocculating area, and clear liquid enters circulation cleaning liquid zone, the slurry after oxidizing, flocculating Liquid is drawn from oxidizing, flocculating area bottom enters subsequent processing units through outer comb line；
（4）Oxidizing gas enters from circulation cleaning liquid zone, and filter medium is sprayed and passed through from the nozzle of oxidizing gas distributor pipe, Dust particles on oxidizing, flocculating area filter medium are blown afloat, the slurries that the dust and oxidizing gas blown afloat is rotated are taken away, Dust acts on coacervating large particle under the effect of gravity to oxidizing, flocculating area bottom deposit, into oxidizing, flocculating area with flocculant Sulfite oxidation in slurries is sulfate by oxidizing gas, keeps the COD of desulfurization wastewater up to standard；
（5）Clear liquid into circulating clear liquid area after filter media is mixed with fresh water and alkaline solution in circulation cleaning liquid zone It is drawn afterwards from circulation cleaning liquid zone bottom, the directly outer row of a small amount of clear liquid is to reduce the salinity of circulating clear liquid, remaining clear liquid is through cycle Enter cooler after clear liquid pump supercharging, enters spraying zone through a cooler clear liquid part after cooling, after atomizer is atomized It is contacted with flue gas adverse current and desulfurization is dusted to flue gas, another part clear liquid flows through liquid distribution trough and enters tower tray area, in tower tray It is upper to come into full contact with the deep desulfuration for strengthening mass transfer effect realization flue gas with flue gas, and will be micro- between 0.1 μm in flue gas ~ 5 μm Small dust particle capture is got off, and realizes the depth dedusting of flue gas, flue gas by a large amount of mist droplets entrained by spraying zone also by Clear liquid on tower tray captures, and reduces the segregational load of mist eliminating zone.
In the method for the present invention, step（1）The flue gas is that fire coal boiler fume, coal-fired plant flue gas, catalytic cracking are urged Agent regenerated flue gas, Furnace flue gas, coking flue gas or steel sintering flue gas etc..The flue gas pipeline I and fume pipe The ratio that line II enters the amount of flue gas is 20 ~ 500；Circulating clear liquid and the ratio of flue gas are 5 ~ 50L/Nm in spraying zone3, preferably compare Example is 8 ~ 25L/Nm3, 3 ~ 15L/Nm of ratio of circulating clear liquid and flue gas in tower tray area3。
In the method for the present invention, step（2）With（5）The alkaline solution be selected from sodium hydroxide solution, calcium hydroxide solution, In magnesium hydroxide solution, sodium carbonate liquor, sodium sulfite solution, sodium citrate solution, lime stone slurry, ammonium hydroxide or seawater etc. It is one or more of.
In the method for the present invention, step（2）With（4）The oxidizing gas be one kind in air, oxygen, ozone etc. or Several, preferably oxidizing gas is air.
In the method for the present invention, step（2）With（4）The oxidizing gas flowrate is according to the slurries chemistry after flocculation concentration Oxygen demand（COD）It is adjusted, COD Con trolling index is ≯ 60mg/L.
In the method for the present invention, step（2）With（4）The flocculant is aluminum sulfate, alum, sodium aluminate, ferric trichloride, sulphur Sour ferrous iron, ferric sulfate, aluminium polychloride, polyaluminium sulfate, polymer phosphate aluminium, poly-ferric chloride, bodied ferric sulfate, polymer phosphate Iron, poly- phosphorus iron chloride, poly- phosphorus aluminium chloride, ferric-polysilicate, poly-silicic acid iron sulfate, polysilicate sulfuric acid aluminium, polyaluminum sulfate ferric-aluminum chloride, The one kind polymerizeing in Polyferric Sulfate silicon flocculant, Al-fe Co Polymer Inorganic Coagulant, polysilicon acid flocculant, polyacrylamide flocculant etc. Or it is several, the addition of flocculant is 0.05 ~ 2kg/m3。
In the method for the present invention, step（3）Slurry pH value after the oxidizing, flocculating is controlled in 7 ~ 9, pH on-line detectors Positioned at outside slurries on comb line, the pH value of desulfurization slurry is controlled by adjusting the regulating valve on alkaline solution line I.
In the method for the present invention, step（3）The liquid level differences of the both sides partition board I is 0.5 ~ 6m, and oxidizing, flocculating area Liquid level is higher than the liquid level of circulation cleaning liquid zone.
In the method for the present invention, step（3）The oxidizing, flocculating area liquid level is by the regulating valve in outer row's slurry line It is controlled.
In the method for the present invention, step（3）The circulation cleaning liquid zone liquid level by the regulating valve on fresh water pipeline into Row control.
In the method for the present invention, step（3）~（5）The described circulation cleaning liquid zone pH value control is 6 ~ 11, the control of preferable ph Ranging from 7 ~ 8, pH on-line detectors are located on the pump entry pipeline of bottom of tower, by adjusting the adjusting on alkaline solution line II Valve carrys out the pH value of control loop clear liquid.
In the method for the present invention, step（3）The outer plasma discharge liquid and step（5）The outer liquid that clears enters subsequent processing Unit, can be used for preparing or produce gypsum, sodium sulfite, sodium hydrogensulfite, magnesium sulfite, magnesium sulfate, magnesia, sodium sulphate, The products such as ammonium sulfate, ammonium hydrogen sulfate may also pass through qualified discharge after filter.
Compared with the prior art, the advantages of the present invention are as follows：
1, wastewater treatment is divided into oxidizing, flocculating area by the present invention in desulfurizing tower lower part setting wastewater treatment area by two pieces of partition boards With circulation cleaning liquid zone, the oxidation, flocculation and concentration of desulfurization wastewater are realized in oxidizing, flocculating area；Wastewater treatment area center it is vertical Filter medium is set on partition board, and the filtering that desulfurization slurry is realized using the liquid level difference of vertical clapboard both sides as motive force is grasped Make.Circulatory mediator of the circulating clear liquid being obtained by filtration as dust-removal and desulfurizing, due to containing without containing dust or dust in circulating clear liquid Amount is very low, uses the slurries containing dust as the circulatory mediator of dust-removal and desulfurizing compared to existing dust-removal and desulfurizing technology, this method is removed Dirt is efficient.Inlet flue gas is divided into two-way by the present invention, wherein the high-temperature flue gas entered by oxidizing, flocculating area bottom is from arc-shaped Flue gas branch pipe tangentially sprays, and pushes the rotation of dust-removal and desulfurizing waste liquid, the material in oxidizing, flocculating area is made to be sufficiently mixed contact, Be conducive to the progress of oxidizing, flocculating reaction, the dust and sulfur-containing oxide in flue gas also obtain certain absorption, while also fully High-temperature flue gas waste heat is utilized, the moisture in dust-removal and desulfurizing waste water is made largely to vaporize, desulfurization wastewater is realized in oxidizing, flocculating area Preliminary concentrate, reduce the energy consumption of subsequent cell.Meanwhile oxidizing gas of the invention not directly enters oxidizing, flocculating area, But introduced from circulation cleaning liquid zone, filter medium is rinsed using oxidizing gas, eliminates flushing device.The present invention saves Conventional mixing plant and filter plant, wastewater treatment process has been gone to greatly reduce device without expending the additional energy Investment and operating cost.
2, reverse taper deformation diameter is arranged in the present invention between tower tray area and spraying zone, advantageously reduces tower tray area gas velocity, by force Change gas-liquid mass transfer effect, improves flue gas in the efficiency of dust collection and desulfuration efficiency in tower tray area, entrainment is reduced, to reduce mist eliminating zone Load；Cone-shaped reducing is arranged with mist eliminating zone in flue gas emission area, is conducive to the flow velocity for improving flue gas, and the gas velocity of flue gas is bigger, It is higher that flue gas leaves the rising height behind flue gas emission area, is more conducive to the diffusion of flue gas, thus plume is shorter.
3, the present invention completes flue gas ash removal, flue gas desulfurization and wastewater treatment in a tower, realizes flue gas depth and removes Dirt, desulfurization and waste water COD qualified discharge triple functions, each functional area coordinated, technological process is short, and occupation of land is greatly reduced Area significantly reduces the expense needed for plant construction, transformation.
Description of the drawings
Fig. 1 is fume desulfurizing tower structural schematic diagram of the present invention.
Fig. 2 is partition board A of the present invention to structural schematic diagram.
Fig. 3 is wastewater treatment area B of the present invention to structural schematic diagram.
Fig. 4 is present invention process flow diagram.
Fig. 5 is the demister structural schematic diagram of the present invention.
Fig. 6 is a kind of rectification channel and the schematic cross-section with groove outer barrel in the demister of the present invention.
Fig. 7 is another rectification channel and the schematic cross-section with raised outer barrel in the demister of the present invention.
Fig. 8 is that the demister middle section of the present invention is the groove schematic diagram that circular arc and straightway are constituted.
In figure：1- flue gas emissions area；2- cone-shaped reducings；3- mist eliminating zones；4- tower trays area；5- reverse taper deformation diameters；6- sprays Drench area；6-1- circulating clear liquid pipelines II；6-2- flue gas pipelines I；7- wastewater treatments area；8- oxidizing, flocculatings area；8-1- liquid level gauges I； 8-2-alkaline solution line I；8-3-flocculant line；8-4-arranges slurry line outside；8-5-flue gas pipeline II；9- circulation cleanings Liquid zone；9-1-liquid level gauge II；The fresh water pipelines of 9-2-；9-3- alkaline solution lines II；9-4-oxidizing gas pipeline；9-5 Clear liquid draws pipeline；9-6-clears liquid pipe line outside；10- smoke inlets；11- demisters；12- liquid distribution troughs；12-1- is recycled Clear liquid pipeline I；13- tower trays；14- spray pipes；15- atomizers；16- blow vents；17- flue gas branch pipes；18- oxidizing gas Distributor pipe；19- partition boards II；20- partition boards I；21- filter mediums；22- sealing strips；23- fastening screws；24- wind turbines；25- is cooled down Device；26- circulation cleaning liquid pumps；
Wherein, 11-1- mist eliminating zones tower tray；11-2- riseies；11-3- rectifications channel；11-4- outer barrels；11-5- covers plate；11- 6- grooves；11-7- protrusions.
Specific implementation mode
Below in conjunction with drawings and examples, the present invention will be described in detail.
The fume desulfurizing tower of the present invention, is from top to bottom followed successively by flue gas emission area 1, mist eliminating zone 3, tower tray area 4, spraying zone 6 With wastewater treatment area 7；The flue gas emission area 1 is connected with mist eliminating zone 3 by cone-shaped reducing 2, and 3 lower section of mist eliminating zone is tower tray Area 4, tower tray area 4 are connected with spraying zone 6 by reverse taper deformation diameter 5, and 6 lower section of spraying zone is wastewater treatment area 7；The waste water 7 center for the treatment of region is divided by one piece of vertical partition board I 20 for oxidizing, flocculating area 8 and circulation cleaning liquid zone 9, wherein oxidizing, flocculating area 8 It is connected to spraying zone 6, the top of circulation cleaning liquid zone 9 is by partition board II 19 by circulation cleaning liquid zone 9 and oxidizing, flocculating area 8 and spraying zone 6 It is completely separated.
The partition board I 20 is arranged at least one opening, preferably 1 ~ 20, more preferably 1 ~ 4, opening area be every The 10% ~ 90% of 20 areas of plate I, preferably 50% ~ 70%；Filter medium 21 is fixed in the opening of partition board I 20；The filtering is situated between Matter 21 is natural fiber, synthetic fibers, glass fiber, reticular structure, preferably metal mesh made of wire, and mesh size is 0.1 ~ 1000 μm, preferably 5 ~ 100 μm；Filter medium 21 is fixed on by sealing strip 22, fastening screw 23 in the opening of partition board 20.
19 both ends partition board II are connect with partition board I 20 and 9 tower wall of circulation cleaning liquid zone respectively, partition board I 20 and partition board The angle of 19 junctions II is generally 45 ~ 165 °, preferably 120 ~ 150 °.The partition board I 20 and partition board II 19 and tower wall Between seal, avoid demarcation strip both sides air-liquid short circuit.
The tower diameter ratio in the mist eliminating zone 3 and flue gas emission area 1 is 1.2 ~ 5；The tower in the tower tray area 4 and spraying zone 6 Diameter ratio is 1.2 ~ 3.
Exhanst gas outlet is arranged in 1 top of flue gas emission area, the flue gas for discharging purification.
Defogging equipment is arranged in the mist eliminating zone 3, the drop for removing flue gas carrying, and the defogging equipment can be One or more of vortex-flow and defrosting device, wet-type electrostatic defroster, mesh mist eliminator or deflector type demister etc..
One or more layers tower tray 13 can be arranged in the tower tray area 4, and the preferably tower tray number of plies is 2 ~ 6 layers；The tower tray can Tower tray is combined for a type of tower tray or multiple types, including float valve tray, screen hole type tower tray, is oriented to screen hole type tower tray, is solid Tongue tower tray, directional float tray or combined trapezoid spray tray etc. come into full contact with the deep desulfuration strengthened mass transfer and realize flue gas for gas-liquid, will The minute dusts particle capture between 0.1 μm ~ 5 μm in flue gas gets off to realize the depth dedusting of flue gas, and flue gas is carried A large amount of mist droplets capture the segregational load for reducing mist eliminating zone 3.
Liquid distribution trough 12 is set between the tower tray area 4 and mist eliminating zone 3, and liquid distribution trough 12 connects circulation cleaning liquid pipe Line I 12-1, for circulating clear liquid to be evenly dispersed to tower tray 13.
One or more layers spray pipe 14 is arranged in 6 top of spraying zone, when Multi-layer sprinkling pipeline 14 is set, spray tube The distance between line 14 is 0.5 ~ 5m, and preferred distance is 1 ~ 2.5m；The spray pipe 14 connects circulating clear liquid pipeline II 6- 1, multiple atomizers 15 are provided on spray pipe 14；The spraying zone 6 is small after atomization for circulating clear liquid to be atomized Drop is contacted with flue gas adverse current, removes the dust and sulfur dioxide carried in flue gas；6 lower part of the spraying zone setting flue gas enters Mouth 10, for connecting flue gas pipeline I 6-2.
The oxidizing, flocculating area 8 is separately connected alkaline solution line I 8-2, flocculant line 8-3 close to tower wall side With liquid level gauge I 8-1；Flow control valve is set on the alkaline solution line I 8-2, for filling alkali into desulfurization wastewater Property solution adjusts its pH value；The flocculant line 8-3 makes for filling flocculant into desulfurization wastewater in desulfurization wastewater Little particle dust cohesion is at bulky grain.
8 bottom of oxidizing, flocculating area connects flue gas pipeline II 8-5 and outer row's slurry line 8-4；The fume pipe Line II 8-5 extend to 8 inside of oxidizing, flocculating area and are parallel to partition board I20, the flue gas pipeline II 8-5 inside oxidizing, flocculating area 8 Horizontal distribution several groups flue gas branch pipe 17, preferably 2 ~ 4 groups, flue gas branch pipe 17 and flue gas pipeline II 8-5 connect successively from down to up It is logical；Every group of flue gas branch pipe 17 is made of 2 ~ 8 flue gas branch pipes 17, and flue gas branch pipe 17 is arc-shaped, every group of flue gas branch pipe 17 are uniformly distributed and rotation direction is identical in the horizontal direction；Flue gas from the direction that flue gas branch pipe 17 sprays be circular arc tangential direction, Flue gas high speed, which sprays, pushes slurries rotation, is stirred for the slurries to oxidizing, flocculating area 8, makes the material in oxidizing, flocculating area It is uniformly mixed, and dust particles on filter medium 21 is rinsed；Outer row's slurry line 8-4 is used for oxidizing, flocculating Subsequent processing units are drained into outside slurries afterwards, and flow control valve and pH meter are set on outer row's slurry line 8-4；The flow tune The flow of plasma discharge liquid outside the Signal Regulation that section valve feed back according to liquid level gauge I 8-1, the liquid level for controlling the flocculation zone that liquefies；It is described PH meter be used to measure the pH value of outer plasma discharge liquid, and signal via controller is fed back into the flow on alkaline solution line I 8-2 Regulating valve.
The circulation cleaning liquid zone 9 is connected with fresh water pipeline 9-2, alkaline solution line II9-3, oxygen close to tower wall side The property changed gas line 9-4 and liquid level gauge II9-1；Flow control valve is set on the fresh water pipeline 9-2, according to liquid level gauge II The flow of the Signal Regulation fresh water of 9-1 feedbacks, is used for the liquid level of control loop clear liquid area 9；The alkaline solution line II Flow control valve is provided on 9-3, the flow for adjusting the alkaline solution filled to circulation cleaning liquid zone 9；The oxidisability Gas line 9-4 is connected with wind turbine 24, and extends to 20 sides partition board I of circulation cleaning liquid zone 9, with oxidizing gas distributor pipe 18 are connected；Several nozzles are provided on the oxidizing gas distributor pipe 18, nozzle faces Jie of the filtering on partition board I 20 Matter 21, oxidizing gas spray from nozzle and pass through filter medium 21, by the dust particles on 8 filter medium 21 of oxidizing, flocculating area It blows afloat, the slurries that the dust and oxidizing gas blown afloat is rotated are taken away, and dust is with flocculant effect coacervating large particle in weight To 8 bottom deposit of oxidizing, flocculating area under force effect, into oxidizing, flocculating area 8 oxidizing gas by the sulphite oxygen in slurries Sulfate is turned to, keeps the COD of desulfurization wastewater up to standard.
Blow vent 16 is set in the 9 top tower wall of circulation cleaning liquid zone, for ensureing that 9 pressure of circulation cleaning liquid zone is steady, It avoids pressure oscillation excessive and filter medium 21 is damaged.
9 bottom of the circulation cleaning liquid zone connection clear liquid draws pipeline 9-5, draws pipeline and is divided into two-way, pipeline connects all the way Liquid pipe line 9-6 is cleared outside connecing, another way pipeline connects circulation cleaning liquid pump 26, pH meter, circulation cleaning liquid pump 26 are provided on the pipeline Circulating clear liquid pipeline I 12-1 and circulating clear liquid pipeline II 6-1 are connected through cooler 25；The pH meter is for measuring circulation cleaning The pH value of liquid, and measuring signal via controller is fed back to the regulating valve of alkaline solution line II 9-3.
Present invention preferably employs the demister 11 of such as lower structure, demister 11 includes several demisting components arranged side by side, often A demisting component includes riser 11-2 and outer barrel 11-4, and outer barrel 11-4 is arranged in the outside of riser 11-2, preferably with liter Tracheae 11-2 is on the same axis；Riser 11-2 is fixed on mist eliminating zone tower tray 11-1, the top setting envelope of riser 11-2 Cover board 11-5；Several rectification channel 11-3 are uniformly arranged on the circumference of riser 11-2, rectification channel 11-3 is along riser 11-2 The tangential direction level of outer wall is embedded in, side wall Is and riser 11-2 tube wall phase of the rectification channel 11-3 close to the sides outer barrel 11-4 It cuts, another side wall II intersects with riser 11-2 tube walls, and each rectification channel direction of rotation 11-3 is identical；At the top of the 11-3 of rectification channel It is flushed with capping plate 11-5, bottom is intersected with riser 11-2 tube walls.
In the demister of the present invention, the rectification channel 11-3 generally settings 1 ~ 12, preferably 4-8.Rectification channel The wall thickness of 11-3 is preferably identical as the wall thickness of riser 11-2.
In the demister of the present invention, the length l of rectification channel 11-3 is the length of side wall II, and width w is rectification channel 11- Maximum horizontal range between 3 two sides, height h are the maximum normal distance between the top and bottom rectification channel 11-3；It is wherein long Spend 2 ~ 5 times, preferably 3 ~ 4 times that l is width w；The cross sectional shape of rectification channel 11-3 be rectangle, ellipse, circle, it is trapezoidal or The combination of one or more of semicircle etc., one or more of preferably rectangular, oval or round combination.Rectification channel The size of 11-3 determined according to actual operating mode or design requirement by those skilled in the art, such as the rectification channel 11- 3 height h is generally 20~600mm, preferably 100~300mm；The width w of rectification channel 11-3 is generally 10~200mm, Preferably 20~100mm.The total sectional area of rectification channel 11-3 is 0.2 ~ 0.9 times of riser 11-2 cross-sectional areas, preferably 0.3 ~ 0.6 times of riser 11-2 cross-sectional areas.
In the demister of the present invention, the ends side wall II of the rectification channel 11-3 can be neat with riser 11-2 inner walls It is flat（Such as Fig. 2）Or it extend into certain distance m inside riser 11-2（Such as Fig. 3）, m is 0.1 ~ 0.9 times of length l, preferably 0.3 ~ 0.6 times.When the ends side wall II of rectification channel 11-3 are flushed with riser 11-2 inner walls, rectification channel 11-3 bottom ends Also it is flushed with riser 11-2 inner walls（Such as Fig. 2）；When the side wall II of rectification channel 11-3 is extend into inside riser 11-2 centainly When distance m, rectification channel 11-3 bottom ends are flushed with side wall end（Such as Fig. 3）.
In the demister of the present invention, rectification channel 11-3 distance from bottom tower trays 11-1 has a certain distance A, and distance A is 20~ 200mm, preferably 40~80mm.
In the demister of the present invention, the lower ends riser 11-2 are concordant with tower tray 11-1 or are less than tower tray 11-1 a distances, The two airtight connection；The diameter of riser 11-2 and the percent opening of tower tray 11-1 can according to actual operating mode or design requirement, It is determined by those skilled in the art.
In the demister of the present invention, the rectification channel 11-3, capping plate 11-5 and riser 11-2 can be welded on Together or global formation.
In the demister of the present invention, the outer barrel 11-4 is preferably cylinder, and outer barrel 11-4 diameters D is that riser 11-2 is straight 1.5-6 times of diameter d, preferably 2-3 times.Upper edge the certain distance P, distance P that the upper edge of outer barrel 11-4 is higher by riser 11-2 be 1~8 times of rectification channel 11-3 height h, preferably 2~5 times.The lower edge of outer barrel 11-4 has certain distance B apart from tower tray 11-1, And less than rectification channel 11-3 lower edge, distance B of the outer barrel 11-4 lower edges away from tower tray 11-1 be 5~100mm, preferably 20~ 50mm.The overall height H of outer barrel 11-4 is 2.5~10 times, preferably 3~5 times of rectification channel 11-3 height.The shape of outer barrel 11-4 Shape can also be the combination of one or more of cone cylinder, inversed conical drum or reducing cylinder etc..
In the demister of the present invention, groove 11-6 and/or protrusion 11-7 is arranged in the inner surface of the outer barrel 11-4.Protrusion 11-7 or groove 11-6 are parallel with the axis of outer barrel 11-4, or can form an angle with axis.The groove 11-6 or The section of raised 11-7 can also be the suitable shapes such as rectangle, triangle or circle.
In the demister of the present invention, the inner surface of the outer barrel 11-4 is preferably provided with cross sectional shape as shown in Figure 4 The section of groove 11-6, groove 11-6 are made of a circular arc and straight line section；Wherein circular arc and outer barrel 11-4 inner surfaces The intersection point of circumference does the tangent line of circular arc and circumference respectively, and the angle between tangent line is α, and α is 5 ° ~ 70 °, preferably 10 ° ~ 40 °；Circle The tangent line of circular arc and the angle of straightway done at arc and straightway intersection point is β, and β is 30 ° ~ 110 °, preferably 45 ° ~ 90 °. The depth Z of groove 11-6, i.e. circular arc are outer barrel 11-4 with the shortest distance on straightway intersection point to outer barrel 11-4 inner surface circumference 0.1 ~ 0.7 times of wall thickness, preferably 0.3 ~ 0.5 times；The intersection point and straightway and outer barrel of circular arc and outer barrel 11-4 inner surface circumference Arc length X between the intersection point of 11-4 inner surface circumference is the 1/80 ~ 1/6 of outer barrel 11-4 inner surface circumference.
In the demister of the present invention, toothing or waveform knot can also be arranged in the lower ending opening of the outer barrel 11-4 Structure is dripped from the inner wall of outer barrel 11-4 at continuous flow to be more conducive to the liquid isolated.
The junction of each component of demister of the present invention ensures sealing, does not generate gas leak phenomenon.The demister of the present invention, work When making, the gas of entrained drip enters riser 11-2 from tower tray 11-1 lower spaces, and Vapor Entrainment liquid phase rises, and encounters capping Gas phase flow direction changes after plate 11-5, i.e., is changed to horizontal or level of approximation direction by ascent direction, and part droplet It since effect of inertia and capping plate 11-5 collide, and is attached on capping plate 11-5, the drop of attachment becomes larger, and works as liquid When dripping the resultant force for arriving climbing power and surface tension of liquid that the gravity that its own is generated is more than gas greatly, drop is just from capping plate It is separated on the surfaces 11-5, completes first time gas-liquid separation；The gas of entrained drip is along horizontal or level of approximation direction Into rectification channel 11-3, since rectification channel 11-3 has certain length, and rectification channel 11-3 total sectional areas are less than liter gas Pipe 11-2 cross-sectional areas, the gas of the more dispersed entrained drip of script directional velocity, after entering rectification channel 11-3, speed Direction is changed to the direction along rectification channel 11-3, directional velocity comparison rule and concentration, and since circulation area reduces, makes folder Speed increases after guttiferous gas enters rectification channel 11-3.When the directional velocity of the gas of entrained drip changes, part liquid Drop collides with rectification channel 11-3 inner walls, and is attached on the 11-3 inner walls of rectification channel, and then is constantly flowed through rectification and led to The gas blowout rectification channel 11-3 of road 11-3 simultaneously falls, and completes second of gas-liquid separation.Meanwhile in the 11-3 of rectification channel, Since the gas velocity direction of entrained drip changes, part droplet issues raw mutually collision in inertia force effect, and droplet is poly- It is integrated into big drop, and speed increases when the gas stream rectified channel 11-3 of entrained drip, exacerbates the movement of drop, improves The probability that droplet mutually collides makes droplet be easier to assemble and become big drop, and with gas with larger speed Flow out rectification channel 11-3.The gas of the entrained drip flowed out from rectification channel 11-3 has larger speed, directional velocity ratio Compared with concentration, and the drop carried secretly is bigger, and continuation collides with outer barrel 11-4 inner walls, changes the flow direction of gas again, I.e. the gas of entrained drip along the rectification channel directions 11-3 by being changed to flow along the circumferencial direction of outer barrel 11-4 inner walls.Due to The gas velocity of entrained drip is larger, and rotates and flow up along the outer barrel 11-4 inner walls for opening up fluted 11-6, therefore meeting Generate obvious shaving effect.The shaving effect refers to that the high-speed gas of entrained drip is revolved along outer barrel 11-4 inner walls When turning to flow up, drop is constantly thrown toward outer under the action of inertia force, and drop enters groove 11-6 and along groove 11-6 Interior arc section movement can make the arc surface that drop continues on groove 11-6 do and smoothly transport since angle α is 5 ° ~ 70 ° It is dynamic, aggregation is contacted between drop and is become larger, until encountering, straightway is hindered, assembles the drop to become larger and is hit strongly with straightway wall surface It hits, and is attached on the straightway of outer barrel 11-4 inboard wall grooves 11-6, drop continues to assemble and become larger, and then along outer barrel 11-4 Wall goes downstream；And gas then continues that high speed is kept to flow up along the rotation of outer barrel 11-4 inner walls, realizes gas-liquid point for the third time From, and reduce entrainment.By above-mentioned rectification, acceleration and shaving effect, fluid is made to realize drop in flow process With the separation of gas.
Embodiment
A kind of flue-gas dust-removing and desulfurization tower is from top to bottom followed successively by flue gas emission area 1, mist eliminating zone 3, tower tray area 4, spraying zone 6 With wastewater treatment area 7, flue gas emission area 1 is connected with mist eliminating zone 3 by cone-shaped reducing 2, and 3 lower section of mist eliminating zone is tower tray area 4, tower Panel 4 is connected with spraying zone 6 by reverse taper deformation diameter 5, and 6 lower section of spraying zone is wastewater treatment area 7.
Wet-type electrostatic defroster 11 is set in mist eliminating zone 3, liquid distribution trough 12 is set to 11 lower section of wet-type electrostatic defroster, Tower tray area 4 is set to 12 lower section of liquid distribution trough, and tower tray area 4 is arranged 4 floor tower tray, selects sieve pore tower tray altogether；Spraying zone 6 is arranged altogether 3 layers of spray pipe 14, the distance between spray pipe 14 are 2m, and atomizer 15 is uniformly arranged on spray pipe 14.
The center of wastewater treatment area 7 is divided by one piece of vertical partition board I 20 for oxidizing, flocculating area 8 and circulation cleaning liquid zone 9, Middle oxidizing, flocculating area 8 is connected to spraying zone 6, and circulation cleaning liquid zone 9 and oxidation are wadded a quilt with cotton by partition board II 19 in 9 top of circulation cleaning liquid zone Coagulation zone 8 and spraying zone 6 are completely separated, and partition board I 20 is connected with partition board II 19 by welding manner, partition board I 20, partition board II 19 It is connected by welding manner between tower wall.There are one openings for setting on partition board I20, positioned at opening for 8 side of oxidizing, flocculating area Mouth region domain is fixed with the metal mesh 21 that aperture is 100 μm, and metal mesh 21 is fixed on separation by sealing strip 22 and fastening screw 23 On plate I 20；8 bottom of oxidizing, flocculating area is provided with flue gas pipeline II 8-5, flue gas pipeline II 8-5 and extends to oxidizing, flocculating area 8 Part on be provided with 5 groups of flue gas branch pipes 17, every group of flue gas branch pipe 17 is uniformly distributed in the horizontal direction and rotation direction is identical, every group Flue gas branch pipe 17 is made of 4 flue gas branch pipes 17, flue gas branch pipe 17 be it is arc-shaped,；Circulation cleaning liquid zone 9 is arranged close to tower wall side Oxidizing gas pipeline 9-4, oxidizing gas pipeline 9-4 extend to 20 sides partition board I of circulation cleaning liquid zone 9, with oxidisability gas Body distributor pipe 18 is connected；Several nozzles are provided on the oxidizing gas distributor pipe 18, nozzle faces on partition board I 20 Filter medium 21；It is provided with blow vent 16 in the tower wall on 9 top of circulation cleaning liquid zone.
A kind of method of flue gas ash removal, desulfurization and wastewater treatment, the flue gas of the present embodiment processing are to contain dust, titanium dioxide The catalytic cracking catalyst regenerated flue gas of sulphur, it is not limited to such flue gas.The flue gas ash removal, desulfurization and waste water of the present embodiment The method of processing specifically includes the following contents：
（1）The flue-gas temperature come from On Fcc Waste Heat Boiler is 185 DEG C, and flue gas divides two-way to enter fume desulfurizing tower, passes through all the way Flue gas pipeline I 6-2 enter from 6 lower part of spraying zone of fume desulfurizing tower, and another way is through flue gas pipeline II 8-5 from fume desulfurizing tower 8 bottom of oxidizing, flocculating area enter through the slurries in oxidizing, flocculating area 8, wherein flue gas pipeline I 6-2 and flue gas pipeline II Flue gas flow ratio is 20 in 8-5, and two-way flue gas converges to be carried in the circulating clear liquid counter current contacting removing flue gas with spraying zone 6 afterwards Most of dust and sulfur dioxide enter tower tray area 4 across the flue gas of spraying zone 6, and depth is carried out in tower tray area 4 and circulating clear liquid Dust-removal and desulfurizing, purified flue gas discharge after 3 demisting of mist eliminating zone from flue gas emission area 1, the cigarette discharged from flue gas emission area 1 Temperature degree is 52 DEG C, dust content 7mg/Nm3, SO2Content is 18mg/Nm3, it is better than GB 31570-2015《Petroleum refining work Industry pollutant emission standard》Regulation（Catalytic cracking catalyst regenerated flue gas particulate matter ≯ 50mg/Nm3, SO2≯100mg/Nm3； Key area particulate matter ≯ 30mg/Nm3, SO2≯50mg/Nm3）；
（2）The desulfurization slurry for absorbing dust and sulfur dioxide enters oxidizing, flocculating area 8, by adjusting sodium hydroxide solution （32w%）Flow come control 8 desulfurization wastewater of oxidizing, flocculating area pH value be 7.5 ~ 8, desulfurization slurry is through flue gas pipeline II 8-5 It is sufficiently mixed with air, polysilicon acid flocculant and sodium hydroxide solution under the stirring action of the flue gas of entrance, in desulfurization slurry Sulphite is oxidized to sulfate, and the little particle dust in desulfurization slurry flocculates into bulky grain, while having certain temperature Flue gas makes the moisture in desulfurization slurry constantly volatilize, and salinity gradually increases；
（3）By adjusting the liquid level in the flow control oxidizing, flocculating area 8 of outer plasma discharge liquid 8-6, by adjusting fresh water 9-2's The liquid level of flow control circulation cleaning liquid zone 9 makes the liquid level in oxidizing, flocculating area 8 and the liquid level difference of circulation cleaning liquid zone 9 be maintained at 1.0 ~ 2.0m, for desulfurization slurry under the action of partition board I20 both sides liquid level differences, the metal mesh 21 flowed through on partition board I 20 realizes solid-liquid It detaches, the dust particles in desulfurization slurry, which are filtered, stays in oxidizing, flocculating area 8, and clear liquid enters circulation cleaning liquid zone 9, oxidation wadding Slurries after solidifying are drawn from 8 bottom of oxidizing, flocculating area enters subsequent processing units through outer comb line；
（4）Enter from the air of wind turbine 24 from circulation cleaning liquid zone 9, sprays and pass through from the nozzle of oxidizing gas distributor pipe 18 Metal mesh 21 blows afloat the dust particles on 8 metal mesh 21 of oxidizing, flocculating area, what the dust and oxidizing gas blown afloat was rotated Slurries are taken away, and dust acts on coacervating large particle under the effect of gravity to oxidizing, flocculating area bottom deposit, into oxygen with flocculant Sulfite oxidation in slurries is sulfate by the oxidizing gas of change flocculation zone 8, keeps the COD of desulfurization wastewater up to standard；
（5）Enter the sodium hydroxide solution of circulation cleaning liquid zone 9 by adjusting（32wt%）Flow carrys out 9 desulfurization of control loop clear liquid area The pH value of waste water is 7.0 ~ 7.5, and clear liquid and the fresh water and sodium hydroxide that circulating clear liquid area 9 is entered after the filtering of metal mesh 21 are molten Liquid is drawn after the mixing of circulation cleaning liquid zone 9 from 9 bottom of circulation cleaning liquid zone, and the directly outer row of a small amount of clear liquid is to reduce the sulphur of circulating clear liquid Sour sodium content, remaining clear liquid are cooled to 40 DEG C after the supercharging of circulation cleaning liquid pump 26 into cooler 25, after the cooling of cooler 25 A clear liquid part enter spraying zone 6, contacted with flue gas adverse current desulfurization be dusted to flue gas after the atomization of atomizer 15, separately A part of clear liquid flows through liquid distribution trough 12 and enters tower tray area 4, is come into full contact with flue gas on tower tray 13 and strengthens mass transfer effect reality The deep desulfuration of existing flue gas, and the minute dusts particle capture between 0.1 μm in flue gas ~ 5 μm is got off, realize the depth of flue gas Dedusting is spent, flue gas is also captured by the clear liquid on tower tray 13 by a large amount of mist droplets entrained by spraying zone 6, reduces and remove The segregational load of fog-zone 3.

Claims (27)

1. a kind of fume desulfurizing tower, it is characterised in that：From top to bottom it is followed successively by flue gas emission area, mist eliminating zone, tower tray area, spraying zone With wastewater treatment area；Exhanst gas outlet is set at the top of the flue gas emission area；Defogging equipment is arranged in the mist eliminating zone；Described One or more layers tower tray is arranged in tower tray area；The wastewater treatment area center is oxidizing, flocculating by one piece of I points vertical of partition board Area and circulation cleaning liquid zone, wherein oxidizing, flocculating area are connected to spraying zone, by partition board II by circulating clear liquid at the top of circulation cleaning liquid zone Area and oxidizing, flocculating area and spraying zone are completely separated, and blow vent is arranged on circulation cleaning liquid zone top drum wall；The partition board I settings At least one opening, opening area are the 10% ~ 90% of partition board I areas；Filter medium is fixed in the opening of partition board I；The oxygen Change flocculation zone bottom connection flue gas pipeline II and outer row's slurry line；The flue gas pipeline II is extended to inside oxidizing, flocculating area And it is parallel to partition board I, the horizontal distribution several groups flue gas branch pipes successively from down to up of the flue gas pipeline II inside oxidizing, flocculating area.
2. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The filter medium is natural fiber, synthesis Fiber, glass fiber, reticular structure made of wire, mesh size are 0.1 ~ 1000 μm, preferably 5 ~ 100 μm.
3. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The both ends partition board II respectively with partition board I and The tower wall connection of circulation cleaning liquid zone, partition board I and the angle of the junctions partition board II are generally 45 ~ 165 °, preferably 120 ~ 150 °.
4. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The flue gas emission area passes through cone with mist eliminating zone Bodily form reducing is connected, and the tower diameter ratio in the mist eliminating zone and flue gas emission area is 1.2 ~ 5.
5. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：Tower tray area passes through reverse taper deformation diameter with spraying zone It is connected；The tower diameter ratio in the tower tray area and spraying zone is 1.2 ~ 3.
6. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The defogging equipment is vortex-flow and defrosting device, wet One or more of formula electrostatic precipitator, mesh mist eliminator or deflector type demister.
7. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The defogging equipment structure is as follows：Demister Including several demisting components arranged side by side, each demisting component includes riser（11-2）And outer barrel（11-4）, outer barrel（11- 4）It is arranged in riser（11-2）Outside, preferably with riser（11-2）On the same axis；Riser（11-2）It is fixed on On mist eliminating zone tower tray 11-1, riser（11-2）Top setting capping plate（11-5）；Riser（11-2）Circumference on uniformly Several rectification channels are set（11-3）, rectification channel（11-3）Along riser（11-2）The tangential direction level of outer wall is embedded in, whole Circulation road（11-3）Close to outer barrel（11-4）The side wall I and riser of side（11-2）Tube wall is tangent, another side wall II and liter gas Pipe（11-2）Tube wall intersects, each rectification channel（11-3）Direction of rotation is identical；Rectification channel（11-3）Top and capping plate（11- 5）It flushes, bottom and riser（11-2）Tube wall intersects.
8. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The tower tray is float valve tray, screen hole type tower Disk, the one or more combinations being oriented in screen hole type tower tray, solid tongue tower tray, directional float tray or combined trapezoid spray tray.
9. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：Liquid is set between the tower tray area and mist eliminating zone Body distributor, liquid distribution trough connects circulating clear liquid pipeline I, for circulating clear liquid to be evenly dispersed to tower tray.
10. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The spraying zone top is arranged one layer or more Layer spray pipe；When Multi-layer sprinkling pipeline is arranged, the distance between spray pipe is 0.5 ~ 5m；The spray pipe connection follows Ring clear liquid pipeline II is provided with multiple atomizers on spray pipe；Smoke inlet I, connection is arranged in the spraying zone lower part Flue gas pipeline I.
11. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The oxidizing, flocculating area is close to tower wall side It is separately connected alkaline solution line I, flocculant line and liquid level gauge I；Flow-rate adjustment is set on the alkaline solution line I Valve.
12. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：Every group of flue gas branch pipe is by 2 ~ 8 flue gases Branch pipe forms, and flue gas branch pipe is arc-shaped, and every group of flue gas branch pipe is uniformly distributed in the horizontal direction and rotation direction is identical.
13. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The circulation cleaning liquid zone is close to tower wall side It is connected with fresh water pipeline, alkaline solution line II, oxidizing gas pipeline and liquid level gauge II；It is set on the fresh water pipeline Set flow control valve；It is provided with flow control valve on the alkaline solution line II, is filled for adjusting to circulation cleaning liquid zone Alkaline solution flow.
14. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The oxidizing gas pipeline and wind turbine phase Even, and the sides partition board I of circulation cleaning liquid zone are extended to, be connected with oxidizing gas distributor pipe；The oxidizing gas distribution Several nozzles are provided on pipe, nozzle faces the filter medium on partition board I.
15. fume desulfurizing tower described in accordance with the claim 1, it is characterised in that：The circulation cleaning liquid zone bottom connects clear liquid Pipeline is drawn, pipeline is drawn and is divided into two-way, pipeline connection is outer all the way clears liquid pipe line, and another way pipeline connects circulation cleaning liquid pump, PH meter is provided on the pipeline, circulation cleaning liquid pump connects circulating clear liquid pipeline I and circulating clear liquid pipeline II through cooler；Described PH meter is used to measure the pH value of circulating clear liquid, and measuring signal via controller is fed back to the regulating valve of alkaline solution line II.
16. a kind of method of flue gas ash removal, desulfurization and wastewater treatment, it is characterised in that including following content：（1）Flue gas divides two-way Into fume desulfurizing tower, enter all the way from the spraying zone lower part of fume desulfurizing tower through flue gas pipeline I, another way is through flue gas pipeline II The slurries in oxidizing, flocculating area are entered through from the oxidizing, flocculating area bottom of fume desulfurizing tower, after two-way flue gas converges and are sprayed The most of dust and sulfur dioxide carried in the circulating clear liquid counter current contacting removing flue gas in area, passes through the flue gas of spraying zone to enter Tower tray area carries out depth dust-removal and desulfurizing in tower tray area and circulating clear liquid, and purified flue gas is after mist eliminating zone demisting from flue gas It discharges discharge region；（2）The desulfurization slurry for absorbing dust and sulfur dioxide enters oxidizing, flocculating area, enters through flue gas pipeline II Flue gas stirring action under be sufficiently mixed with oxidizing gas, flocculant and alkaline solution, the sulphite in desulfurization slurry It is oxidized to sulfate, the little particle dust in desulfurization slurry flocculates into bulky grain, while there is the flue gas of certain temperature to make to take off Moisture in sulphur slurries constantly volatilizees, and salinity gradually increases；（3）Desulfurization slurry is under the action of partition board I both sides liquid level differences, stream It realizes and is separated by solid-liquid separation through the filter medium on partition board I, the dust particles in desulfurization slurry, which are filtered, stays in oxidizing, flocculating area, Clear liquid enters circulation cleaning liquid zone, and the slurries after oxidizing, flocculating are drawn from oxidizing, flocculating area bottom enters subsequent processing through outer comb line Unit；（4）Oxidizing gas enters from circulation cleaning liquid zone, is sprayed from the nozzle of oxidizing gas distributor pipe and filtering is passed through to be situated between Matter blows afloat the dust particles on oxidizing, flocculating area filter medium, the slurries band that the dust and oxidizing gas blown afloat is rotated It walks, for dust with flocculant effect coacervating large particle under the effect of gravity to oxidizing, flocculating area bottom deposit, oxidizing gas will Sulfite oxidation in slurries is sulfate, keeps the COD of desulfurization wastewater up to standard；（5）Enter cycle after filter media The clear liquid of clear liquid area is drawn after circulation cleaning liquid zone mixes from circulation cleaning liquid zone bottom with fresh water and alkaline solution, a small amount of clear liquid Directly outer row is to reduce the salinity of circulating clear liquid, remaining clear liquid enters cooler after the supercharging of circulation cleaning liquid pump, through cooler A clear liquid part after cooling enters spraying zone, contacted with flue gas adverse current after atomizer is atomized flue gas is dusted it is de- Sulphur, another part clear liquid flow through liquid distribution trough and enter tower tray area, come into full contact with flue gas on tower tray, will be small in flue gas Dust particles and flue gas are captured by a large amount of mist droplets entrained by spraying zone.
17. according to the method for claim 16, it is characterised in that：Step（1）The flue gas is fire coal boiler fume, combustion One in coal-fired plant's flue gas, catalytic cracking catalyst regenerated flue gas, Furnace flue gas, coking flue gas or steel sintering flue gas Kind is a variety of.
18. according to the method for claim 16, it is characterised in that：The flue gas pipeline I and flue gas pipeline II enters cigarette The ratio of the amount of gas is 20 ~ 500；Circulating clear liquid and the ratio of flue gas are 5 ~ 50L/Nm3 in spraying zone, circulating clear liquid in tower tray area With 3 ~ 15L/Nm3 of ratio of flue gas.
19. according to the method for claim 16, it is characterised in that：The alkaline solution is selected from sodium hydroxide solution, hydrogen Calcium oxide solution, magnesium hydroxide solution, sodium carbonate liquor, sodium sulfite solution, sodium citrate solution, lime stone slurry, ammonium hydroxide Or one or more of seawater.
20. according to the method for claim 16, it is characterised in that：The oxidizing gas is air, oxygen or ozone One or more of.
21. according to the method for claim 16, it is characterised in that：The flocculant be aluminum sulfate, alum, sodium aluminate, Ferric trichloride, ferrous sulfate, ferric sulfate, aluminium polychloride, polyaluminium sulfate, polymer phosphate aluminium, poly-ferric chloride, polyaluminum sulfate Iron, polymer phosphate iron, poly- phosphorus iron chloride, poly- phosphorus aluminium chloride, ferric-polysilicate, poly-silicic acid iron sulfate, polysilicate sulfuric acid aluminium, polymerised sulphur Sour ferric-aluminum chloride, polymerization Polyferric Sulfate silicon flocculant, Al-fe Co Polymer Inorganic Coagulant, polysilicon acid flocculant or polyacrylamide flocculation One or more of agent.
22. according to the method for claim 16, it is characterised in that：Step（3）Slurry pH value after the flocculation concentration Control is located in 7 ~ 9, pH on-line detectors on the outer comb line of slurries, is controlled by adjusting the regulating valve on alkaline solution line I The pH value of desulfurization slurry processed.
23. according to the method for claim 16, it is characterised in that：Step（3）The liquid level difference of the both sides partition board I is 0.5 ~ 6m, the liquid level in oxidizing, flocculating area are higher than the liquid level of circulation cleaning liquid zone.
24. according to the method for claim 16, it is characterised in that：Step（3）The oxidizing, flocculating area liquid level by Regulating valve in outer row's slurry line controls.
25. according to the method for claim 16, it is characterised in that：Step（3）The flushing water in the oxidizing, flocculating area sprays Shower pipe is periodically rinsed the filter medium on partition board I, and 0.5 ~ 2h is divided between washing time.
26. according to the method for claim 16, it is characterised in that：Step（3）The circulation cleaning liquid zone liquid level by Regulating valve on fresh water pipeline is controlled.
27. according to the method for claim 16, it is characterised in that：Step（3）~（5）The circulation cleaning liquid zone pH value control System is located in 6 ~ 11, pH on-line detectors on the pump entry pipeline of bottom of tower, by adjusting the adjusting on alkaline solution line II Valve carrys out the pH value of control loop clear liquid.
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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003066525A1 (en) * 2002-02-08 2003-08-14 F.L. Smidth Airtech A/S Improvement of flue gas desulfurization gypsum-dewatering through crystal habit modification by carboxylic acids
CN201454396U (en) * 2009-02-26 2010-05-12 成都信息工程学院 Spray-type desulfurization tower with integrated absorption, oxidation, crystallization, mist elimination and temperature reduction
CN205796937U (en) * 2016-06-16 2016-12-14 武汉国力通能源环保股份有限公司 A kind of integrated purifying device of sulfide hydrogen off-air

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003066525A1 (en) * 2002-02-08 2003-08-14 F.L. Smidth Airtech A/S Improvement of flue gas desulfurization gypsum-dewatering through crystal habit modification by carboxylic acids
CN201454396U (en) * 2009-02-26 2010-05-12 成都信息工程学院 Spray-type desulfurization tower with integrated absorption, oxidation, crystallization, mist elimination and temperature reduction
CN205796937U (en) * 2016-06-16 2016-12-14 武汉国力通能源环保股份有限公司 A kind of integrated purifying device of sulfide hydrogen off-air

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