CN101637685A - Comprehensive treatment method of sulfur-containing flue gas - Google Patents
Comprehensive treatment method of sulfur-containing flue gas Download PDFInfo
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- CN101637685A CN101637685A CN200910305992A CN200910305992A CN101637685A CN 101637685 A CN101637685 A CN 101637685A CN 200910305992 A CN200910305992 A CN 200910305992A CN 200910305992 A CN200910305992 A CN 200910305992A CN 101637685 A CN101637685 A CN 101637685A
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Abstract
The invention belongs to the technical field of chemical industry, in particular to a comprehensive treatment method of sulfur-containing flue gas. The comprehensive treatment method comprises the following steps: (a) dedusting through a bath tower; (b) desulphurizing through a desulphurizing and absorbing tower, wherein , dewatering the sulfur-containing flue gas after being treated by water washing and dedusting in the step (a). When the method is applied to purify the sulfur-containing flue gas, the efficiency of dedusting and removing sulfur dioxide and hydrogen sulfide reaches 100 percent, thus zero discharge of pollutants in exhaust smoke can be realized.
Description
Technical field
The invention belongs to chemical technology field, particularly the sulfur-containing smoke gas integrated conduct method.
Background technology
Sulfur-containing flue gas purifying generally includes water washing dedust and two steps of desulfurization, traditional water scrubber washing process is that flue gas enters from the tower bottom, washings enter from tower top, contact with flue gas is reverse, dust in flue gas is washed, enter washings, the dust-laden washings go out from the scrubbing tower underflow, reach desirable cleaning dust and cooling-down effect, need a large amount of washings.
The flue gas desulfurization technique of studying both at home and abroad at present reaches kind more than 200, obtain commercial Application also have 40 surplus more than the kind.The method of commercial Application is mainly: 1) lime/lime stone doctor treatment, comprise dry method, semidry method, wet method, and account for about 80% of total flue gas desulfur device.The lime/lime stone sulfur removal technology was developed at first in the 60-70 age in last century, was that external industrialization developed country develops for strict day by day at that time fume emission index, and its advantage is that lime or lime stone source are abundant, low price.Weak point is many, the one, to content of sulfur dioxide than higher (as 5000mg/Nm
3) flue gas because the solubility of calcium hydroxide is very little, and be difficult to adapt to; The 2nd, a large amount of gypsum inferior that desulfurization produces can't be handled, if near do not have operable unit such as cement plant, have to abandon, so the lime/lime stone method also is the method for abandoning; The 3rd, the gypsum of abandoning inferior, also have the high chloride ion-containing waste water that produces in the sweetening process etc., environment is produced secondary pollution; The 4th, calcium sulfite that this method generates in sweetening process and calcium sulfate easily are deposited on equipment, pipeline and the desulfurizing tower internals, cause system jams, also can cause device parking etc. when serious.2) other sulfur method comprises electric desulfurization, charcoal absorption desulfurization etc., accounts for 20% of total desulfurization greatly.These methods respectively have characteristics, and its weak point is also had nothing in common with each other, and get up all to exist following shortcoming but sum up: desulfuration efficiency all is difficult near 100%, and sulfur dioxide is difficult to reach zero-emission in the discharged gas fume; Product after the desulfurization does not almost obtain actual utilization; Operating cost is than higher.
Summary of the invention
First technical problem to be solved by this invention provides the integrated conduct method of the high sulfur-containing smoke gas of a kind of desulfuration efficiency.
The technical scheme that addresses the above problem comprises step a, water scrubber dedusting, b, desulfuration absorbing tower desulfurization; Carry out processed behind the step a sulfur-containing smoke gas water washing dedust.
Further, described sulfur-containing smoke gas dust content is 50～200mg/Nm
3, 40～60 ℃ of flue-gas temperatures.Sulfur-containing smoke gas contacts in that washing section packing layer and washings are reverse in the water scrubber, and dust in flue gas enters water.In order not allow the flue gas after the dedusting carry big water gaging in follow-up desulfuration absorbing tower, remove flue gas behind the dust in tower during through the dewatering period packing layer, the water that flue gas is carried all is removed to and only contains saturation water, goes desulfurizing tower to carry out desulfurization then.The washings that contain dust flow at the bottom of the water scrubber, extract out with circulation cleaning pump at the bottom of the tower, can send the plate and frame filter press press filtration, remove solid particulate matters such as dust wherein after, can return scrubbing tower and use as the washings repetitive cycling.Compare with traditional handicraft, circulation cleaning can be adjusted the sprinkle density of washings flexibly, and cleaning dust and cooling-down effect have clear improvement; The 2nd, water-saving result is obvious; The 3rd, be difficult for occluding device, can long-term operation.
Receive after the sulfur-containing smoke gas washing the washings solids removed by filtration particle that contains dust after, use as washings.
Further, described step b is: the gas after step a handles with the desulfurizing agent desulfurization after gas-liquid separation be purified gas.
Described desulfurizing agent is at least a in aqueous solution of sodium bisulfite, the aqueous sodium carbonate.The rich solution pH value that step b desulfurizing agent absorbs behind the sulfur dioxide was directly used as desulfurizing agent in 5.6～6.0 o'clock.
The rich solution that step b desulfurizing agent absorbs behind the sulfur dioxide can be used for producing sodium sulfite, may further comprise the steps:
C, neutralization
Rich solution adds sulfate radical chemical agent (being preferably brium carbonate), adds sodium carbonate liquor then and makes the pH value reach 9.0, regulates the pH value with sodium hydroxide solution again and reaches 10.0;
D, filtration
With step c receive solution filter, filtering gained filtrate is sodium sulfite solution;
E, crystallization
The sodium sulfite solution of steps d concentrates under vacuum condition, separates out crystal;
F, drying
Step e receive the sodium sulfite crystal dry under 260～300 ℃ of temperature, after the cooling promptly.
Steps d is preferably goes into the press filtration of sheet frame filter press with the solution pump after the neutralization end, filters out solid impurities such as precipitation.If the solid impurity removal effect of filtrate is bad, can filter repeatedly 2～3 times.
The vacuum condition of step e concentrates by realizing that by the vacuum concentration systems vacuum concentration systems is mainly returned equipment such as pond, vacuum draw pump, filter centrifugal and forms by vacuum concentration pot, steam heater, mother liquor pond, mother liquor down.
The solid-liquid drain hole of vacuum concentration pot bottom is connected with filter centrifugal by the mother liquor pond, and the bottom of filter centrifugal is returned the pond by mother liquor and is connected with the mother liquor return port of vacuum concentration pot; Steam heater connects the upper end circulation solution import and the lower end circulation solution of vacuum concentration pot respectively and extracts mouth out; The vacuum draw pump connects the vacuum concentration pot top.
Start the vacuum draw pump among the step e, steam is extracted a mouthful outflow out from vacuum concentration pot top vacuum, is condensed into condensate water with condensate cooler, and condensate water can be sent to obtain solution.
Step e receive crystal on contain adhesional wetting water, be transported to pneumatic drier with screw rod conveyor, sodium sulfite drying machine cooler after dehydrating cooling back packing, warehouse-in export trade.
Second technical problem to be solved by this invention provides a kind of water scrubber, comprises tower body, and the tower body hypomere is the washing section that random packing is housed, and the tower body epimere is the dewatering period that structured packing is housed, and separates with dividing plate between two sections; Sulfur-containing smoke gas inlet and washings outlet are positioned at the water scrubber lower end, and the inlet of water is positioned at the washing section upper end, and gas vent is positioned at the water scrubber top.Described dividing plate has hole or breather pipe.
Wherein, random packing is Pall ring or cascade ring, and the random packing material is stainless steel or pottery, and structured packing is ripple orifice plate or ripple silk net, and the structured packing material is RPP plastics, vinylon, polyvinyl chloride or stainless steel.
The 3rd technical problem to be solved by this invention provides a kind of desulfuration absorbing tower, comprise tower body, gas feed and rich solution outlet are positioned at the tower body lower end, the desulfurizing agent inlet is positioned at tower body middle part or top, random packing and structured packing mixed packing in the tower, the top of tower is provided with gas-liquid separator, purifies back gas and discharges through gas-liquid separator.
Wherein, random packing is Pall ring, cascade ring or θ ring, and structured packing is ripple orifice plate or ripple silk net, and the structured packing material is RPP plastics, vinylon, polyvinyl chloride or stainless steel.
Sulfurous gas flows in absorbing desulfurizing tower from bottom to top, contacts in that filling surface is reverse with desulfurizing agent.At this moment, sulfur in smoke is desulfurized agent and absorbs, and generates sodium hydrogensulfite with reactions such as sodium carbonate in the desulfurizing agent, sodium sulfites, thereby is changed in the liquid phase by gas phase, and gas obtains desulfurizing and purifying.
The middle part of desulfuration absorbing tower or top all can spray desulfurizing agent, also can the middle part, top sprays desulfurizing agent simultaneously.Desulfurizing agent is at least a in aqueous solution of sodium bisulfite, the aqueous sodium carbonate.Be preferably at desulfuration absorbing tower middle part spray aqueous solution of sodium bisulfite, contain the aqueous solution of sodium hydrogensulfite and sodium carbonate at desulfuration absorbing tower top spray.Wherein aqueous sodium carbonate is fresh preparation (being also referred to as lean solution), and aqueous solution of sodium bisulfite can freshly be prepared, and also can absorb solution (being also referred to as rich solution) behind the sulfur dioxide with aqueous sodium carbonate.Rich solution is extracted out by circulating pump at the bottom of desulfuration absorbing tower, rich solution pH value can be used as the circulation desulfurization agent and enters desulfuration absorbing tower from the spray liquid inlet at desulfuration absorbing tower middle part and repeat to absorb sulfur dioxide the sulfurous gas at 5.6～6.0 o'clock, rich solution also can further be produced the sodium sulfite product.
The integrated conduct method of sulfur-containing smoke gas of the present invention has the following advantages:
1) desulfurization dust-removing efficiency height, dedusting, removal sulfur dioxide, depriving hydrogen sulphide efficient are up to 100%, dust, sulfur dioxide equal size are zero in the purification flue gas, can realize zero release of pollutant in the smoke evacuation, because the discharged gas fume depuration quality after this PROCESS FOR TREATMENT is very high, can be used as the unstripped gas that industry and food-grade carbon-dioxide reclaim;
2) utilize circulation absorption technique control operation condition, solved sulphite is become sulfate by dioxygen oxidation in the flue gas problem;
3) water scrubber and desulfuration absorbing tower have all designed dewatering period, and direct separating and dehydrating in tower in washing or after absorbing does not need knockout drum is set specially, has reduced project investment;
4) solid particulate matter that may bring into of flue gas enters circulation solution system, just may be deposited on filler, pipeline and the equipment wall, results in blockage, and can cause when serious that whole device stops.Therefore on the washings pipeloop, be provided with plate and frame filter press, in time to remove by filter flue dust and the dust in the water; Advancing on the doctor solution pipeloop of desulfuration absorbing tower to be provided with high-accuracy filter, so that timely filtering solid particles thing.Fundamentally solved the problem that other sulfur removal technology stops at the easy blocking device of the most normal appearance in position such as pipeline, wall, tower internals and filler, fully assurance device long period even running.
5) utilize sulfur in smoke to produce the anhydrous sodium sulfite product, make the sulphur in the flue gas obtain recycling, can not cause the waste of sulphur resource, utilize the qualified anhydrous sodium sulfite product of sulphur dioxide production that removes, sulphur is got utilization; The anhydrous sodium sulfite product quality of producing meets the quality requirement of national certified products and Grade A.
6) production anhydrous sodium sulfite product process unit investment cost is few, the SO of recovery
2Behind the anhydrous sodium sulfite production marketing of producing, can offset operating cost fully, therefore we can say that this technology is zero run cost technology; And non-secondary pollution is clean environment-friendly treating process.
Description of drawings
Fig. 1 is the flue gas desulfurization technique schematic diagram, 3 water scrubbers, 5 desulfuration absorbing towers.
Fig. 2 is the flue gas desulfurization technique schematic diagram, 1 cyclone dust collectors, and 2 electric cleaners, 3 water scrubbers, 4 plate and frame filter press, 5 desulfuration absorbing towers, 6 filters are the part of selecting use according to actual conditions in the frame of broken lines.
Fig. 3 is a preparation anhydrous sodium sulfite process schematic representation, 7 neutralizing tanks, 8 solution preparing tanks, 9 sodium carbonate liquor storage tanks, 10 plate and frame filter press, 11 vapor recycle water condensation coolers, 12 vacuum concentration pots, 13 steam heaters, 14 filter centrifugals, 15 mother liquor ponds, 16 vacuum buffer are divided flow container, 17 vavuum pump circulation water pots, 18 mother liquors return the pond.
The specific embodiment
For the lower (＜1000mg/Nm of dust content
3) can directly give water scrubber 3 to carry out the water washing dedust cooling, technological process is as shown in Figure 1.
For dust content than higher (＞1000mg/Nm
3) sulfur-containing smoke gas or barite (barium sulfate) and celestine (strontium sulfate) high temperature reduction rotary kiln sulfur-containing smoke gas, before carrying out desulfurizing and purifying, need pre-dust removal process, for example coal and oil boiler smoke, oil plant catalyst regeneration sinter fume, coke are calcined rotary kiln flue gas, metal smelt flue gas etc. to dust content than higher sulfur-containing smoke gas, technological process as shown in Figure 2
Sulfur-containing smoke gas enters from water scrubber 3 lower ends, and the cavity of water from 3 two sections fillers of water scrubber enters, and sulfur-containing smoke gas obtains removing flue gas behind the dust through the washing section packing layer, the filler by dewatering period again, the sulfurous gas after obtaining dewatering in water scrubber 3 tops; Receive to such an extent that contain the washings of dust at the bottom of the water scrubber; Sulfurous gas after the dehydration enters desulfuration absorbing tower 5 from the bottom, tower middle part or top spray desulfurizing agent, and the gas after the desulfurization is purified gas behind the gas-liquid separator separatory of desulfuration absorbing tower top; Obtain the rich solution after desulfurizing agent absorbs sulfur dioxide at the bottom of desulfuration absorbing tower 5 towers.
Rich solution is extracted out by circulating pump at the bottom of desulfuration absorbing tower 5 towers, and rich solution pH value was filtered the back at 5.6～6.0 o'clock through filter 6 and entered desulfuration absorbing tower 5 as the circulation desulfurization agent from the spray liquid inlet at desulfuration absorbing tower 5 middle parts and repeat to absorb sulfur dioxide the sulfurous gas
Receive at the bottom of water scrubber 3 towers the washings that contain dust send plate and frame filter press 4 press filtrations, remove solid particulate matter wherein after, can return water scrubber 3 and use as washings.
Dust content must be removed the dust more than 95% in the flue gas with dry method earlier than higher sulfur-containing smoke gas, could further adopt wet method to remove remaining dust.For example, barite and celestine high temperature reduction rotary kiln flue gas adopt cyclone dust collectors 1 to remove the wherein dust more than 70% earlier, use electric cleaner 2 or sack cleaner again, dust in flue gas is removed to more than 95%, just can advance the cooling of water scrubber 3 water washing dedusts at last.Because contain barium sulphide and strontium sulfide in the dust of barite and celestine high temperature reduction rotary kiln flue gas, these compounds can be soluble in water with after washings contact.After the circulating cleaning solution that contains barium sulphide and strontium sulfide contacts carbon dioxide in the flue gas, will react water-fast compounds such as generating brium carbonate and strontium carbonate with it, be deposited in associated conduit, equipment wall and filling surface etc., cause that pipeline and filler stop up, and cause the parking of whole desulfurizer.
The gas temperature that water scrubber 3 cats head are discharged can be controlled by the magnitude of recruitment of cooling water in the cat head chilled water unit.Water scrubber 3 bottom liquid level height can be by the control of circulation cleaning pump.
Remove Purge gas directly emptying behind desulfuration absorbing tower 5 top gas-liquid separator separatory of sulfur dioxide.The Purge gas of emptying can make its content of sulfur dioxide meet country and local environmental emission standard by regulating process operation parameter, also can make the content of sulfur dioxide in the efflux gas equal 0.
Fig. 3 is the process schematic representation of preparation anhydrous sodium sulfite, receive at the bottom of desulfuration absorbing tower 5 towers rich solution neutralizing tank 7, add sulfate radical chemical agent (being preferably brium carbonate), adding sodium carbonate liquor (being stored in sodium carbonate liquor storage tank 9) then makes the pH value reach 9.0, use again sodium hydroxide solution (being stored in solution preparing tank 8) regulate pH value reach receive after 10.0 solution send into plate and frame filter press 10 and filter, filtration gained filtrate is sodium sulfite solution; Sodium sulfite solution concentrates under vacuum condition, separates out crystal, receive crystal on contain adhesional wetting water, and dry under 260～300 ℃ of temperature, promptly get anhydrous sodium sulfite after the cooling.
Adopt screw rod conveyor to be transported to pneumatic drier when crystal is dry, the sodium sulfite drying machine cooler cooling back packing after dehydrating, warehouse-in export trade.
Vacuum condition concentrates down and realizes that by the vacuum concentration systems vacuum concentration systems mainly divides flow container 16, vavuum pump circulation water pot 17 and mother liquor to return pond 18 equipment by neutralizing tank 7, solution preparing tank 8, sodium carbonate liquor storage tank 9, plate and frame filter press 10, vapor recycle water condensation cooler 11, vacuum concentration pot 12, steam heater 13, filter centrifugal 14, mother liquor pond 15, vacuum buffer and forms.
The solid-liquid drain hole of vacuum concentration pot 12 bottoms is connected with filter centrifugal 14 by mother liquor pond 15, and the bottom of filter centrifugal 14 is returned pond 18 by mother liquor and is connected with the mother liquor return port of vacuum concentration pot 12; Steam heater 13 connects the upper end circulation solution import and the lower end circulation solution of vacuum concentration pot 12 respectively and extracts mouth out; Vapor recycle water condensation cooler 11 connects the vacuum concentration pot top.
Start the vacuum draw pump, steam is extracted a mouthful outflow out from vacuum concentration pot 12 top vacuum, be condensed into the gas that is mixed with condensate water with vapor recycle water condensation cooler 11, the gas that is mixed with condensate water divides flow container 16 separatory by vacuum buffer, receive condensate water to be stored in vavuum pump circulation water pot 17 stand-by, can send to obtain solution.
Rich solution pH value is 5.6～6.0, adjusts the pH value at neutralizing tank 7 and reaches at 10.0 o'clock, and the sodium hydrogensulfite in the rich solution has all changed into sodium sulfite.Because general oxygen content is 6～7% in the flue gas, content of sulfur dioxide is a trace, has only hundreds of to 5000mg/Nm
3, oxygen is more than 35 times of sulfur dioxide normally, although therefore taked the measure of some anti-oxidation in solution, sulphite is become the situation of sulfate to be difficult to avoid by dioxygen oxidation.According to industrial production, if do not remove sodium sulphate, then in the anhydrous sodium sulfite of Sheng Chaning the content of sodium sulphate generally up to 5～6% (quality).In order to reduce sodium sulphate content, need take off adding sulfate radical chemical agent to remove sulfate radical in neutralization stage.Iron content as fruit product is higher, or during frowziness, can add an amount of iron removing reagent and acticarbons such as vulcanized sodium after neutralization, stir about 20 minutes.
Receive at the bottom of water scrubber 3 towers the washings that contain dust send plate and frame filter press 4 press filtrations, remove can send behind the solid particulate matter wherein neutralizing tank 7 carry out as acid hot water in and sedimentation.
Embodiment 1
The equipment setting of present embodiment is shown in Fig. 2,3.
1, the pre-dedusting of flue gas
The mixed flue gas temperature of celestine high temperature coal reduction flue gas, Crouse's sulfuric acid tail gas incineration flue gas, carbonators pressure release incineration flue gas is 200 ℃, becomes to be grouped into (mol) to be:
CO
2??12～18％；O
2??6～7％；N
2+Ar??75～82％；
SO
24000mg/Nm
3More than; Dust 22～25g/Nm
3
Earlier make in the flue gas dust content reduce to 5000mg/Nm with cyclone dust collectors
3, with electric cleaner dust content in the flue gas is reduced to 600mg/Nm again
3, 150～220 ℃ of flue-gas temperatures.Deliver to water scrubber then and wash the cooling dedusting, standard state flow 24000Nm
3/ h, operating mode flow 41582.42m
3/ h.The water scrubber process conditions are as follows:
1) advances tower flue gas
Flue-gas temperature: 150～220 ℃
Exhaust gas dust content:＜200mg/Nm
3
2) washings
The temperature of washings: 30～40 ℃
The washings leaving water temperature that contains dust at the bottom of the tower: 40～50 ℃
Liquid level control: 1.5 ± 0.2m at the bottom of the tower
3) random packing
Random packing can be adopted Pall ring, cascade ring etc., and material is stainless steel or pottery, according to concrete flue gas compositing characteristic, passes through Lectotype and calculation.
Structured packing is ripple orifice plate or ripple silk net, and material can adopt RPP plastics, vinylon, polyvinyl chloride or stainless steel.
4) go out tower flue gas
Overhead streams goes out gas temperature: 40～50 ℃
Fuel gas and dust content:＜10mg/Nm
3
H
2S content: 200～500mg/Nm
3
2, flue gas desulfurization
Washing cat head eluting gas is delivered to the desulfuration absorbing tower bottom, and the desulfuration absorbing tower process conditions are as follows:
1) desulfurizing agent (lean solution, sodium carbonate liquor)
Solution concentration: 20% (mass percent)
2) diffusing windrow
Random packing can be adopted Pall ring, cascade ring, θ ring etc., and structured packing can be adopted regular corrugation orifice plate or ripple silk net, and material can adopt RPP plastics, vinylon, polyvinyl chloride or stainless steel, and two kinds of fillers mix to be placed.Can pass through Lectotype and calculation according to concrete flue gas compositing characteristic.
3) rich solution at the bottom of the tower
PH value: 5.6～6.0
Flow: control according to liquid level at the bottom of the absorption tower
Temperature: 40～50 ℃
Sulfate radical content: less than 7.5g/l
Iron ion content: less than 4mg/l
Color: range estimation does not have color
4) cat head purifies the efflux gas specification of quality
CO
2??12～18％；O
2??6～7％；N
2+Ar??75～82％
Content of sulfur dioxide: be 0 when normally moving, the highest 260mg/Nm when going into operation adjustment
3
Hydrogen sulfide content: 0
Dust content: 0
Water content: saturated
Temperature: 40～50 ℃
3, rich solution neutralization
Add in the sodium carbonate and terminal point: pH value 9.0
NaOH is regulated terminal point: pH value 10.0
Sulfate radical medicament (brium carbonate) addition: per 5 cubic metres of solution add 45～50 kilograms
Deironing medicament addition: per 5 cubes of solution add 4～6 kilograms
Activated carbon powder addition: determine as do not add according to solution colour
Reaction temperature: 40～60 ℃
Mixing speed: 60～80 rev/mins
Reaction time: 2 hours
4, plate compression
Entrance pressure filter solution pressure: greater than 0.8MPa (gauge pressure)
Temperature: 40～80 ℃
5, vacuum concentrates
Thickening temperature: 60 ℃
Vacuum :-0.07MPa
Be sent from the concentration of heart filter solution: solid content 25～30% (mass percent)
6, centrifugal filtration
Filtration temperature: 50～60 ℃
7, dehydrate
Baking temperature: 260～300 ℃
Dried anhydrous sodium sulfite product quality is as shown in table 1:
Table 1
| Analysis project | The HG/T2967-2000 index | The present embodiment product |
| Anhydrous sodium sulfite content | ??≥93％ | ??93～96％ |
| Iron content | ??≤0.02％ | ??0.005～0.02％ |
| The not tolerant content of water | ??≤0.02％ | ??0.005～0.015％ |
| Free alkali content | ??≤0.08％ | ??0.047～0.069％ |
| Sodium sulphate content | ??- | ??2.7～5.3％ |
The anhydrous sodium sulfite that data declaration the inventive method makes in the table 1 meets the requirement of certified products among the industry standard HG/T2967-2000.
Claims (10)
1. the integrated conduct method of sulfur-containing smoke gas comprises step: a, water scrubber dedusting, b, desulfuration absorbing tower desulfurization; It is characterized in that: carry out processed behind the step a sulfur-containing smoke gas water washing dedust.
2. the integrated conduct method of sulfur-containing smoke gas according to claim 1, it is characterized in that: described step b is: the gas after step a handles with the desulfurizing agent desulfurization after gas-liquid separation be purified gas.
3. the integrated conduct method of sulfur-containing smoke gas according to claim 2 is characterized in that: described desulfurizing agent is at least a in aqueous solution of sodium bisulfite, the aqueous sodium carbonate.
4. according to the integrated conduct method of each described sulfur-containing smoke gas of claim 1～3, it is characterized in that: receive after the step a sulfur-containing smoke gas washing the washings solids removed by filtration particle that contains dust after, use as washings.
5. according to the integrated conduct method of claim 2 or 3 described sulfur-containing smoke gas, it is characterized in that: the rich solution pH value that step b desulfurizing agent absorbs behind the sulfur dioxide was directly used as desulfurizing agent in 5.6～6.0 o'clock.
6. according to the integrated conduct method of claim 2 or 3 described sulfur-containing smoke gas, it is characterized in that: the rich solution that step b desulfurizing agent absorbs behind the sulfur dioxide is used to produce sodium sulfite, may further comprise the steps:
C, neutralization
Rich solution adds the sulfate radical chemical agent, adds sodium carbonate liquor then and makes the pH value reach 9.0, regulates the pH value with sodium hydroxide solution again and reaches 10.0;
D, filtration
With step c receive solution filter, filtering gained filtrate is sodium sulfite solution;
E, crystallization
The sodium sulfite solution of steps d concentrates under vacuum condition, separates out crystal;
F, drying
Step e receive the sodium sulfite crystal dry under 260～300 ℃ of temperature, after the cooling promptly.
7. water scrubber comprises tower body, it is characterized in that: the tower body hypomere is the washing section that random packing is housed, and the tower body epimere is the dewatering period that structured packing is housed, and separates with dividing plate between two sections; Sulfur-containing smoke gas inlet and washings outlet are positioned at the water scrubber lower end, and the inlet of water is positioned at the washing section upper end, and gas vent is positioned at the water scrubber top.
8. water scrubber according to claim 7, it is characterized in that: random packing is Pall ring or cascade ring, the random packing material is stainless steel or pottery, and structured packing is ripple orifice plate or ripple silk net, and the structured packing material is RPP plastics, vinylon, polyvinyl chloride or stainless steel.
9. desulfuration absorbing tower comprises tower body, it is characterized in that: gas feed and rich solution outlet are positioned at the tower body lower end, the desulfurizing agent inlet is positioned at tower body middle part or top, random packing and structured packing mixed packing in the tower, the top of tower is provided with gas-liquid separator, purifies back gas and discharges through gas-liquid separator.
10. desulfuration absorbing tower according to claim 9, it is characterized in that: random packing is Pall ring, cascade ring or θ ring, structured packing is ripple orifice plate or ripple silk net, and the structured packing material is RPP plastics, vinylon, polyvinyl chloride or stainless steel.
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