CN105013311A - Flue gas desulfurization dust and mist removal method - Google Patents

Flue gas desulfurization dust and mist removal method Download PDF

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Publication number
CN105013311A
CN105013311A CN201510446627.4A CN201510446627A CN105013311A CN 105013311 A CN105013311 A CN 105013311A CN 201510446627 A CN201510446627 A CN 201510446627A CN 105013311 A CN105013311 A CN 105013311A
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China
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flue gas
liquid
tower
district
dust
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CN201510446627.4A
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Chinese (zh)
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石宝珍
房媛媛
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青岛京润石化工程有限公司
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Priority to CN201510446627.4A priority Critical patent/CN105013311A/en
Publication of CN105013311A publication Critical patent/CN105013311A/en

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Abstract

The present invention provides a flue gas desulfurization dust and mist removal method, a desulfurization medium is an alkaline liquid; a desulfurization tower bottom zone liquid enters respectively from absorption reaction zone bottom and upper parts into a desulfurization tower, a circulating fluid entering from the bottom part is atomized into small liquid drops, parallelly flows with fuel gas, and meanwhile complete sulphide absorption reaction with the countercurrent circulating liquid; by use of alkaline liquid small liquid drop parallel flow capture and venturi particle capture two-level dust removal, and arrangement of surface coalescing and multi-stage cyclone for mist removal, flue gas purification can be achieved.

Description

A kind of removing sulfur, dust and fog from flue gas method
Technical field
The invention belongs to industrial flue gas cleaning technical field, particularly relate to a kind of fume wet type desulphurization dedusting defogging method.
Background technology
Along with the increase year by year of socioeconomic high speed development and energy demand, industrial discharged waste gas amount increases very fast, and along with the increase of sulfur-bearing, nitrogen, dirt waste gas, and national environmental protection regulation also can increasingly stringent, therefore, extremely urgent to the purified treatment of flue gas.Flue gas desulfurization is the most effective and main technological means of control of acid rain and sulfur dioxide pollution, but its general principle is all the absorbent using a kind of alkaline matter as sulfur dioxide.Traditional Wet Flue Gas Desulfurization Technique mainly contains limestone-gypsum method, Sea water respiratory distress syndrome, ammoniacal liquor doctor treatment, double alkali method desulfurizing and sodium alkali desulfurization etc.
Limestone-gypsum doctor treatment, flue gas and loop slurry counter current contacting in absorption tower, there is mass transfer and absorption reaction, sulfur dioxide in flue gas, sulfur trioxide etc. are absorbed, calcium sulfite, calcium sulfate etc. is combined to calcium hydroxide, calcium sulfite, enter circulatory pool, in circulatory pool, carry out forced oxidation and neutralization reaction and form gypsum.Flue gas after washing desulphurization removes droplet through demister, then by flue gas heat-exchange unit from smoke stack emission.This technical maturity, reliable, availability is more than 90%, and energy consumption is low, but capital expenditure is large, and raw sorbent consumption is large, and operating cost is high.
Flue gas desulfurization with seawater has based on seawater that natural alkalescence is gentle rushes ability, and the sulfur dioxide in flue gas, by after Absorption by Sea Water, is converted into sulfate, and a kind of natural constituents of sulfate inherently seawater.First industrial smoke removes the dust in flue gas through electrostatic dust collection equipment, then enter desulfurizing tower, with seawater counter current contacting in filler, and abundant desulfurization.This technique is simple, and do not consume desulfurizing agent, operating cost is low, but very large by region restriction, is not suitable for promoting.
Ammonia-process desulfurization technique adopts ammonia as the technique of the sulfur dioxide in absorbent removing flue gas.Flue gas enters Ta Nei and mixes with reverse contact of ammonia absorbent, sulfur dioxide in flue gas and ammoniacal liquor react and generate ammonium sulfite, flue gas after washing desulphurization is from smoke stack emission after demister dewaters, and desulfurizing byproduct becomes dehydration ammonium sulfate through cyclone, centrifuge dewatering.The method desulfuration efficiency is high, and system is simple, and equipment volume is little, but the price of absorbent ammonia is too high, and high operating cost is the biggest factor to extensive use affecting ammonia desulfurizing process.
Dual alkali comprises sodalime double alkali method, basic aluminum sulfate method etc., the most frequently used is sodalime double alkali method, and it adopts soda sulfur dioxide absorption, and absorbing liquid regenerates with lime again, generate the sediment such as calcium sulfite and calcium sulfate, the solution after regeneration returns absorber and recycles.The method desulfurization degree is high, non-scaling, but flow process is longer, and soda consumes high.
The current domestic main application of sodium alkali desulfurization be the EDV technology of Bel's lattice.EDV Wet Flue Gas Desulfurization Technique is that gas-liquid two-phase first passes through spray district Absorption Desulfurization, then carries out dedusting through filtering module, then gets rid of from chimney after globule separator dewaters.
As can be seen from the pluses and minuses of above several desulfur technology, existing Wet Flue Gas Desulfurization Technique mainly adopts countercurrent spray, alkaline slurry sprays and enters in desulfurizing tower above desulfurizing tower, free settling contacts with flue gas adverse current and realizes desulphurization reaction under gravity, but it is even larger that existing Wet Flue Gas Desulfurization Technique droplet liquid Average equivalent diameter reaches 3-5mm, the contact area of single drop and flue gas is very little, thus have to improve recycle slurry liquid measure to increase desulfurized effect, cause the flow of slurry circulating pump very large, thus increase power of motor, the power consumption of pump increases, operating cost is high.
Summary of the invention
The object of the present invention is to provide a kind of fume wet type desulphurization dedusting defogging method, in the method, akaline liquid, as desulfurization medium, mixes with circulation fluid and after being atomized into drop in desulfurizing tower and smoke contacts, realizes sulfide desulfurization solution absorption; The liquid of fluid zone at the bottom of desulfurizing tower enters desulfurizing tower with top circulation respectively bottom flue gas sulfide absorption reaction district, and the circulation fluid that bottom enters is atomized into droplet and flue gas also flows and the circulated in countercurrent liquid at top completes sulfide absorption reaction simultaneously; Adopt alkali lye droplet and flue gas also to flow and catch dust and the dedusting of venturi particle capture two-stage; Coalescent and the Multi-stage spiral device in surface is set to Exhaust Gas demist, realizes low energy consumption flue gas purification.
Desulfurization principle of the present invention:
The acid-base neutralization that this flue gas desulfurization technique carries out using NaOH as the sulfurous acid solution of desulfurizing agent and the water-soluble generation of sulfur dioxide reacts, and the pH value by regulating the addition of NaOH to regulate circulation fluid.Its chemical equation is as follows:
SO 2+ H 2o----> H 2sO 3(dissolving)
H 2sO 3---->H ++ HS0 3 -(ionization)
Then, sulfurous acid and NaOH react and generate Na 2sO 3, Na 2sO 3with H 2sO 3further reaction generates NaHSO 3, NaHSO 3react with NaOH again and accelerate to generate sodium sulfite; The sodium sulfite part generated recycles as absorbent, and another part goes to discharge as harmless aqueous sodium persulfate solution after Separation of Solid and Liquid, oxidation to treatment unit for waste water:
H 2SO 3+ NaOH----> Na 2SO 3 + 2H 2O
Na 2SO 3 + H 2SO 3---->2NaHSO 3
NaHSO 3+ NaOH ---->2Na 2SO 3+ 2H 2O
Na 2SO 3+ 1/2O 2---->Na 2SO 4
The technical solution adopted in the present invention is: inlet flue gas enters in the smoke inlet section of bottom and enter desulfurized dust collection column after chilling cooling, upwards successively through also, adverse current double acting sulfide absorption reaction district and flow dust catch and venturi catch dedusting area, coalescent vortex-flow and defrosting district, discharge from tower top chimney after purification.
In the present invention, circulation fluid tagma is set at the bottom of desulfurized dust collection column tower, between bottom circulation fluid tagma and desulfurization absorption reaction district at the bottom of tower, liquid-circulating is set, this component loops liquid from circulation fluid tagma extract out through and flow recycle liquid pump boost after, enter in tower by pump discharge pipeline, flow with flue gas after be atomized into droplet with liquid atomiser in tower, realize the contact desulfuriation with sulfur-containing smoke gas.
In the present invention, and send into gas in pipeline before flowing circulating fluid atomizer, realize with gas and flow circulating fluid be atomized into droplet.And flow on circulating fluid pump discharge pipeline dust filter unit be set, enter atomizer after circulation fluid filtration.
In the present invention, circulation fluid tagma and between top, desulfurization absorption reaction district and smoke inlet section, liquid-circulating is set at the bottom of tower, circulating fluid at the bottom of tower is extracted out from circulation fluid tagma by after the boosting of circulated in countercurrent liquid pump, part circulation fluid enters top, desulfurization absorption reaction district in tower through pump discharge pipeline, flow downward, with smoke contacts desulfurization in flow process by gravity and flue gas adverse current be atomized into drop with liquid atomiser in tower after; Part circulation fluid enters inlet flue gas section through pump discharge pipeline, with smoke contacts after inlet flue gas section liquid atomiser is atomized into drop, flue gas is down to saturation temperature.
In the present invention, alkali lye divides two-stage to inject, part alkali lye and position before flowing on recycle liquid pump outlet line atomization inject, position before another part alkali lye is atomized on circulated in countercurrent liquid pump outlet line is injected, alkali lye mixes with circulation fluid after injecting respectively, form desulphurization reaction liquid, so that also stream and adverse current two kinds of modes realize sulfide absorption reaction.
In the present invention, alkali lye divides two-stage to inject, and a part of alkali lye enters liquid level at the bottom of tower in the rising pouring of desulfurized dust collection column tower, and another part alkali lye injects in desulfurized dust collection column venturi tower reactor, and alkali lye mixes with circulation fluid after injecting respectively.
In the present invention, dust in flue gas first with enter bottom desulfurization absorption reaction district and flow the droplet that circulation fluid is atomized into and contact, caught by droplet; And then carry out secondary dust seizure in desulfurization absorption reaction district with except in the shaped Venturi dedusting district between fog-zone; Shaped Venturi dedusting district is arranged in parallel multiple Venturi tube.Above venturi fluid zone and each Venturi exit, circulating fluid is set.Circulating fluid is extracted out from venturi fluid zone, after the boosting of venturi recycle liquid pump, enters in tower through outlet line, with Venturi exit smoke contacts, dust and circulating fluid form larger drop, are deposited in the fluid zone of venturi capture area, return to the fluid zone at the bottom of tower through liquid down-comer.
In the present invention, flue gas is behind desulfurization absorption reaction district, shaped Venturi dedusting district, and flue gas upwards enters coalescent vortex-flow and defrosting district again.Coalescent vortex-flow and defrosting district is in series except fog-zone and vortex-flow and defrosting district by coalescent.Arrange coalescent except fog-zone below coalescent vortex-flow and defrosting district, top arranges cyclonic separation except fog-zone, flue gas first removes fog-zone through coalescent from bottom to top, contact with water-wetted surface that to realize liquid coalescent, and the fluid zone in venturi district is flowed into downwards along surfacing gravity, this district realizes the dedusting of dust-laden droplet coalescence simultaneously; Flue gas upwards enters vortex-flow and defrosting district again, and discharge from chimney after removing remaining liq, liquid flows into the fluid zone in venturi district from pipeline.
In the present invention, vortex-flow and defrosting district forms by organizing vortex-flow and defrosting device arranged side by side more, often organizes vortex-flow and defrosting device and arranges the Multi-stage spiral device of connecting up and down.
In the present invention, coalescent except fog-zone employing coalescence material, tower cross section is divided into numerous bar shaped or grid-shaped exhaust gases passes by coalescence material, and the surperficial vertical direction that coalescence material is formed is installed, and is not more than 45 ° with the angle of plumb line; Coalescence material can be gone up lower leaf and arrange; Each layer coalescence material can be staggered.
In the present invention, vortex-flow and defrosting district is arranged in desulfurized dust collection column, and entrance is located at upper end; Flue gas enters cyclone from upper end, enters chimney in lower end.Flue gas is discharged from chimney after coalescent vortex-flow and defrosting district removing remaining liq, and the liquid separated from vortex-flow and defrosting district flows into the fluid zone in venturi district from pipeline liquid separator tube.
In the present invention, the dust that dedusting area is deviate from enters fluid zone at the bottom of tower with liquid; Discharge with circulated in countercurrent liquid pump outlet line at the bottom of tower.
In the present invention, pass through pipeline injection of ozone at smoke inlet depot siding and/or desulfurizing tower desulfurization absorption reaction district, ozone and nitride reaction realize denitration.
In the present invention, moisturizing adds at desulfurizing tower top venturi portion.
In the present invention, and stream and circulated in countercurrent liquor pump can be designed as multi-channel parallel and enter desulfurizing tower after exporting.
In the present invention, flue gas gas speed in tower is 2.0m/s-5m/s, desulphurization reaction time 3s-9s, and flow that circulation fluid scale of construction accounting is not more than total and stream and adverse current global cycle amount of liquid 20%; The pH value of liquid at the bottom of tower is 6-9; Venturi district liquid pH value is 6-9.
Compared with prior art, the invention has the advantages that:
(1) flue gas of the present invention first carries out Quench cooling before entering tower, reduces the requirement to tower body material, thus decreases investment cost;
(2) inventive desulfurization adopt also, adverse current compound scheme, add gas liquid interfacial area, reduce liquid circulation amount, save operating cost;
(3) dedusting of the present invention adopts and flows seizure and Venturi scrubbing combination technology, improves efficiency of dust collection;
(4) the present invention dewaters and adopts mode that is coalescent and eddy flow combination, decreases the reentrainment of gas, improves demisting efficiency.
Accompanying drawing explanation
Fig. 1 is a kind of schematic diagram of FGD dust collection method of the present invention.
Fig. 2 is the another kind of schematic diagram of FGD dust collection method of the present invention.
In figure: 1, smoke inlet section, 2, desulfurized dust collection column, 3, chimney, 4, and flow recycle liquid pump, 5, circulated in countercurrent liquid pump, 6, venturi recycle liquid pump, 7, and flow atomizer, 8, adverse current atomizer, 9, venturi fluid zone, 10, Venturi tube, 11, coalescent except fog-zone, 12, vortex-flow and defrosting district, 13, dust filter unit, 14, liquid down-comer, 15, fluid separation applications pipe, 16, chilling atomizer, 21, circulation fluid tagma at the bottom of tower, 22, and adverse current double acting desulfurization absorption reaction district, 23, shaped Venturi dedusting district, 24, coalescent vortex-flow and defrosting district, 25, and flow dust seizure and venturi seizure dedusting area, 101, inlet flue gas line, 102, quench liquid line, 103, 104 is ozone injection line, 211, line is extracted out, 212 at the bottom of circulated in countercurrent liquid tower, circulated in countercurrent liquid enters tower line, and 213, and flow extraction line at the bottom of circulation fluid tower, 214, and flow circulation fluid and enter tower line, 215, venturi circulation fluid extracts line out, and 216, venturi circulation fluid enters tower line, and 217, loop slurry sends line to some other department, and 218, 219, 222, 223 is note alkali line, 220, gas inject line, 221, moisturizing line.
In figure: G represents flue gas, W represents moisturizing, and CL represents alkali lye, and SF represents serum recycle liquid, and IA represents gas, arrow representative direction of flow.
Detailed description of the invention
As shown in Figure 1, FGD dust collection method, the smoke inlet section 1 of inlet flue gas 101 in bottom enters desulfurized dust collection column 2 after the cooling of circulation fluid at the bottom of tower 102 chilling, upwards successively through also, adverse current double acting desulfurization absorption reaction district 22 and flow dust catch and venturi catch dedusting area 25, coalescent vortex-flow and defrosting district 24, discharge from tower top chimney 3 after purification;
As shown in Figure 1, circulation fluid tagma 21 is set at the bottom of desulfurizing tower, between bottom circulation fluid tagma 21 and desulfurization absorption reaction district 22 at the bottom of tower, liquid-circulating is set, this component loops liquid 213 from circulation fluid tagma 21 extract out after through and flow recycle liquid pump 4 boosting after, enter in tower by pump discharge pipeline 214, flow with flue gas after be atomized into droplet with liquid atomiser 7 in tower, realize the contact desulfuriation with sulfur-containing smoke gas; And send into gas in pipeline before flowing circulating fluid atomizer, realize with gas and flow circulating fluid be atomized into droplet.And flow on circulating fluid pump discharge pipeline 214 dust filter unit 13 be set, enter atomizer 7 after circulation fluid filtration.
As shown in Figure 1, circulation fluid tagma 21 and between desulfurization absorption reaction top, district 22 and smoke inlet section 1, liquid-circulating is set at the bottom of tower, after circulating fluid 211 at the bottom of tower is extracted out boosted from circulation fluid tagma 21 by circulated in countercurrent liquid pump 5, part circulation fluid enters top, desulfurization absorption reaction district 22 in tower through pump discharge pipeline 212, flow downward, with smoke contacts desulfurization in flow process by gravity and flue gas adverse current be atomized into drop with liquid atomiser 8 in tower after; Part circulation fluid enters inlet flue gas section through pump discharge pipeline 102, with smoke contacts after inlet flue gas section liquid atomiser 16 is atomized into drop, flue gas is down to saturation temperature.
As shown in Figure 1, alkali lye divides two-stage to inject, part alkali lye 218 and position before flowing on recycle liquid pump 4 outlet line 214 atomization inject, position before another part alkali lye 219 is atomized on circulated in countercurrent liquid pump 5 outlet line 212 is injected, alkali lye mixes with circulation fluid after injecting respectively, form desulphurization reaction liquid, so that also stream and adverse current two kinds of modes realize desulphurization reaction.
As shown in Figure 1, dust in flue gas first with enter bottom desulfurization absorption reaction district 22 and flow the droplet that circulation fluid 214 is atomized into and contact, caught by droplet; And then carry out secondary dust seizure in desulfurization absorption reaction district 22 with except in the shaped Venturi dedusting district 23 between fog-zone 24; Shaped Venturi dedusting district 24 is arranged in parallel multiple Venturi tube 10.Venturi fluid zone 9 and each Venturi tube 10 export top and arrange circulating fluid.Circulating fluid 215 is extracted out from venturi fluid zone 9, after venturi recycle liquid pump 6 boosts, enter in tower through outlet line 216, with Venturi exit smoke contacts, dust and circulating fluid form larger drop, be deposited in the fluid zone 9 of venturi capture area, return to the fluid zone at the bottom of tower through liquid down-comer 14.
As shown in Figure 1, flue gas is behind desulfurization absorption reaction district 22, shaped Venturi dedusting district 23, and flue gas upwards enters coalescent vortex-flow and defrosting district 24 again.Coalescent vortex-flow and defrosting district 24 is in series except fog-zone 11 and vortex-flow and defrosting district 12 by coalescent.Arrange coalescent except fog-zone 11 below coalescent vortex-flow and defrosting district 24, top arranges cyclonic separation except fog-zone 12, flue gas first removes fog-zone 11 through coalescent from bottom to top, contact with water-wetted surface that to realize liquid coalescent, and the fluid zone 9 in venturi district is flowed into downwards along surfacing gravity, this district realizes the dedusting of dust-laden droplet coalescence simultaneously; Flue gas upwards enters vortex-flow and defrosting district 11 again, discharges after removing remaining liq from chimney; Liquid flows into the fluid zone 9 in venturi district from pipeline.
As shown in Figure 1, coalescent except fog-zone employing coalescence material, tower cross section is divided into numerous bar shaped or grid-shaped exhaust gases passes by coalescence material, and the surperficial vertical direction that coalescence material is formed is installed, and is not more than 45 ° with the angle of plumb line; Coalescence material can be gone up lower leaf and arrange; Each layer coalescence material can be staggered.Vortex-flow and defrosting district 12 is arranged in desulfurized dust collection column 2, and entrance is located at upper end; Flue gas enters cyclone from upper end, enters chimney 3 in lower end.Flue gas is discharged from chimney 3 after coalescent vortex-flow and defrosting district 24 removes remaining liq, and the liquid separated from vortex-flow and defrosting district 24 flows into the fluid zone 9 in venturi district from pipeline liquid separator tube 15.
As shown in Figure 1, the dust that dedusting area 25 is deviate from enters fluid zone 21 at the bottom of tower with liquid; Discharge with circulated in countercurrent liquid pump 5 outlet line 217 at the bottom of tower.
As shown in Figure 1, pass through pipeline 104 injection of ozone at smoke inlet section 2 pipeline 103 and/or desulfurizing tower desulfurization absorption reaction district 22, ozone and nitride reaction realize denitration.
As shown in Figure 1, moisturizing 221 to add in tower in venturi liquid level 9 at desulfurizing tower top venturi portion.
As shown in Figure 2, alkali lye divides two-stage to inject, and a part of alkali lye 222 enters liquid level at the bottom of tower in the rising pouring of desulfurized dust collection column 2 tower, and another part alkali lye 223 injects in desulfurized dust collection column venturi tower reactor, and alkali lye mixes with circulation fluid after injecting respectively.
Embodiment
Smoke inlet condition: 200000Nm3/h, sulfur dioxide concentration 1260mg/Nm3, dust concentration 180mg/Nm3, temperature 230 DEG C, pressure 4KPa.Sulfur dioxide concentration 52mg/Nm3 in desulfurization and dedusting after funnel exit gas, dust concentration 11.4mg/Nm3.Desulfuration efficiency is 95.9%, and efficiency of dust collection is 93.7%.
Flue gas enters smoke inlet section, at the effect borehole cooling of quench liquid atomizer to saturation temperature 59.8 DEG C, wherein Quench circulating fluid flow rate: 464000kg/h.After cooling, flue gas enters desulfurized dust collection column.Desulfurizing tower diameter: 6m, in tower, from the bottom up, enter and adverse current double acting desulfurization absorption reaction district, and flow employing 45 liquid atomiser, wherein circulating fluid flow rate: 85000kg/h, gas flow is flue gas: 2550 kg/h; Liquid counter-current atomizer adopts three layers, every layer 40 layouts, wherein circulated in countercurrent flow quantity: 1145000kg/h.Flue gas after desulfurization enters shaped Venturi dedusting, and shaped Venturi dedusting district adopts 15 Venturi tubes and 15 liquid atomisers, and wherein venturi circulating fluid flow rate is: 257000kg/h.Then flue gas enters coalescent eddy flow except liquid zone, and coalescent district adopts strip coalescence material, and be staggered, vortex-flow and defrosting device adopts six groups of Multi-stage spiral demisters, and the flue gas behind coalescent vortex-flow and defrosting district is moisture almost nil.Flue gas after dewatering is arranged from chimney.Wastewater flow rate 17950 kg/h of sewage treatment unit is drained into outside device.Fresh soda flow quantity is 1060 kg/h, and desulfurized dust collection column venturi portion injection rate is 74 kg/h, liquid level injection rate 986 kg/h at the bottom of tower.The pH value of circulation fluid at the bottom of tower and venturi circulation fluid is 7.The rate of water make-up of desulfurized dust collection column is: 34642 kg/h.

Claims (11)

1. a removing sulfur, dust and fog from flue gas method, is characterized in that, the flue gas of sulfur-bearing dust-laden purifies through following process implementation:
1. flue gas enters in the smoke inlet section of bottom, desulfurized dust collection column is entered as after quench liquid cooling through the circulating fluid of desulfurizing tower self or external complement liquid, upwards successively through also, adverse current double acting sulfide absorption reaction district and flow dust catch and venturi catch dedusting area, except fog-zone, discharge from tower top chimney after purification;
2. circulation fluid tagma is set at the bottom of desulfurizing tower, between bottom circulation fluid tagma and sulfide absorption reaction district at the bottom of tower, liquid-circulating is set, flow with flue gas after this component loops liquid is atomized into droplet with liquid atomiser in tower, realize the contact with sulfur-containing smoke gas;
3. at the bottom of tower, arrange liquid-circulating between fluid zone and top, desulfurization absorption reaction district, flowing downward by gravity and flue gas adverse current after this component loops liquid is atomized into drop with liquid atomiser in tower returns to fluid zone at the bottom of tower, with smoke contacts in flow process;
4. desulfurization alkali lye respectively and position on stream and circulated in countercurrent liquor pump outlet line before atomization mix with circulation fluid, formation desulfurization absorption reaction liquid, also to flow and adverse current two kinds of modes realize flue gas desulfurization absorption reaction; Or alkali lye fluid zone and/or venturi still tank liquor tagma at the bottom of desulfurized dust collection column tower are injected, alkali lye after injecting respectively with at the bottom of tower and the circulation fluid of venturi mix;
5. dust in flue gas first with enter bottom reaction zone and flow the droplet that circulation fluid is atomized into and contact, caught by droplet; And then carry out secondary dust seizure in desulfurization absorption reaction district with except in the venturi scrubber between fog-zone; Dust and circulating fluid form larger drop, return to the fluid zone at the bottom of tower in the fluid zone being deposited to liquid phase region at the bottom of tower or being deposited to shaped Venturi dedusting district through liquid down-comer;
6. flue gas completes desulfurization, behind shaped Venturi dedusting district, upwards enters except fog-zone again, discharges after removing the liquid carried from chimney; Liquid flows into the fluid zone in venturi district;
7. the dust that absorption reaction district and dedusting area catch enters fluid zone at the bottom of tower with liquid; Discharge from pipeline with component loops liquid at the bottom of tower.
2. a kind of FGD dust collection method as claimed in claim 1, is characterized in that, flue gas gas speed in tower is 2.0m/s-5m/s; Flue gas is at desulfurization absorption reaction district time of staying 3s-9s; And flow circulation fluid scale of construction accounting be not more than and flow and adverse current global cycle amount of liquid 20%; The pH value of liquid at the bottom of tower is 6-9; Venturi district liquid pH value is 6-9.
3. a kind of removing sulfur, dust and fog from flue gas method as claimed in claim 1, is characterized in that, and stream and circulated in countercurrent liquor pump can be designed as multi-channel parallel and enter desulfurizing tower after exporting.
4. a kind of removing sulfur, dust and fog from flue gas method as claimed in claim 1, it is characterized in that, shaped Venturi dedusting district is arranged in parallel multiple Venturi tube.
5. a kind of removing sulfur, dust and fog from flue gas method as claimed in claim 1, is characterized in that, except fog-zone is in series by coalescent district, surface and cyclonic separation district; Flue gas completes desulfurization, behind shaped Venturi dedusting district, enters demist except pool, arranges surface coalescent except fog-zone below this district, and top arranges cyclonic separation except fog-zone; Flue gas from bottom to top first through coalescent except fog-zone, contact with water-wetted surface that to realize liquid coalescent, liquid flows into the fluid zone in venturi district downwards along surfacing gravity, and this district realizes the dedusting of dust-laden droplet coalescence simultaneously; Flue gas upwards enters vortex-flow and defrosting district again, and discharge from chimney after removing remaining liq, liquid flows into the fluid zone in venturi district from pipeline.
6. a kind of removing sulfur, dust and fog from flue gas method as claimed in claim 5, it is characterized in that, tower cross section is divided into numerous bar shaped or grid-shaped exhaust gases passes by coalescent dedusting area coalescence material, and the surperficial vertical direction that coalescence material is formed is installed, and is not more than 45 ° with the angle of plumb line; Coalescence material can be gone up lower leaf and arrange; Each layer coalescence material can be staggered.
7. a kind of removing sulfur, dust and fog from flue gas method as claimed in claim 5, is characterized in that, vortex-flow and defrosting district is set up in parallel many group vortex-flow and defrosting devices, and vortex-flow and defrosting device is arranged in desulfurizing tower, and entrance is located at upper end; Flue gas enters cyclone from upper end, enters chimney in lower end; Often organize vortex-flow and defrosting device to be made up of the Multi-stage spiral device of connecting up and down.
8. a kind of removing sulfur, dust and fog from flue gas method as claimed in claim 1, is characterized in that, at smoke inlet pipeline and/or desulfurizing tower desulfurization absorption reaction district injection of ozone, ozone and nitride reaction realize denitration.
9. a kind of removing sulfur, dust and fog from flue gas method as claimed in claim 1, is characterized in that, and flow on circulating fluid pump discharge pipeline dust filter unit be set, enter atomizer after circulation fluid filtration.
10. a kind of removing sulfur, dust and fog from flue gas method as claimed in claim 1, is characterized in that, arranges circulating fluid above fluid zone or venturi fluid zone and each Venturi exit at the bottom of tower.
11. a kind of removing sulfur, dust and fog from flue gas methods as claimed in claim 1, is characterized in that, and send into gas in pipeline before flowing circulating fluid atomizer, realize with gas and flow circulating fluid be atomized into droplet.
CN201510446627.4A 2015-07-28 2015-07-28 Flue gas desulfurization dust and mist removal method CN105013311A (en)

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CN108117122A (en) * 2016-11-29 2018-06-05 中国石油化工股份有限公司 A kind of processing method and processing unit of sodium method flue gas desulfurization waste-water
CN109550338A (en) * 2017-09-26 2019-04-02 江苏众瑞环保科技有限公司 A kind of flue gas desulfurization denitration dust-removing technique
CN109966879A (en) * 2017-12-28 2019-07-05 上海华畅环保设备发展有限公司 The method and apparatus of sulphur tail gas after incineration sodium method deep desulfuration control alkali
CN110102170A (en) * 2019-04-16 2019-08-09 四川大学 Short route manganese oxide ore pulp sulfur method, desulfuration absorbing tower and manganese Sulphur ressource recovery system based on mini-hydrocyclone separation
CN108117122B (en) * 2016-11-29 2021-03-05 中国石油化工股份有限公司 Treatment method and treatment device for sodium-method flue gas desulfurization wastewater

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CN105251309A (en) * 2015-11-27 2016-01-20 江苏中立环保科技有限公司 Efficient energy-saving static dust and smoke remover and treatment method thereof
CN105771555A (en) * 2016-05-04 2016-07-20 温州佳音环保科技有限公司 Coal burning boiler flue gas cleaning process
CN105944488A (en) * 2016-06-28 2016-09-21 江苏国松环境科技开发有限公司 High-efficiency dust removal equipment
CN108117122B (en) * 2016-11-29 2021-03-05 中国石油化工股份有限公司 Treatment method and treatment device for sodium-method flue gas desulfurization wastewater
CN108117122A (en) * 2016-11-29 2018-06-05 中国石油化工股份有限公司 A kind of processing method and processing unit of sodium method flue gas desulfurization waste-water
CN107281920A (en) * 2017-06-12 2017-10-24 太仓运权化工防腐设备有限公司 A kind of flue gas desulfurization device
CN107233791A (en) * 2017-07-27 2017-10-10 中国石油化工股份有限公司 One kind eliminates catalytic unit desulphurization denitration tower plume method
CN107233791B (en) * 2017-07-27 2020-08-07 中国石油化工股份有限公司 Method for eliminating smoke plume of desulfurization and denitrification tower of catalytic device
CN109550338A (en) * 2017-09-26 2019-04-02 江苏众瑞环保科技有限公司 A kind of flue gas desulfurization denitration dust-removing technique
CN109966879A (en) * 2017-12-28 2019-07-05 上海华畅环保设备发展有限公司 The method and apparatus of sulphur tail gas after incineration sodium method deep desulfuration control alkali
CN110102170A (en) * 2019-04-16 2019-08-09 四川大学 Short route manganese oxide ore pulp sulfur method, desulfuration absorbing tower and manganese Sulphur ressource recovery system based on mini-hydrocyclone separation

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