CN101637685B - Comprehensive treatment method of sulfur-containing flue gas - Google Patents

Comprehensive treatment method of sulfur-containing flue gas Download PDF

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Publication number
CN101637685B
CN101637685B CN2009103059928A CN200910305992A CN101637685B CN 101637685 B CN101637685 B CN 101637685B CN 2009103059928 A CN2009103059928 A CN 2009103059928A CN 200910305992 A CN200910305992 A CN 200910305992A CN 101637685 B CN101637685 B CN 101637685B
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gas
sulfur
tower
desulfurizing agent
solution
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CN2009103059928A
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CN101637685A (en
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郭克雄
郭毛晓春
黄云霞
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成都德美工程技术有限公司
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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

The integrated conduct method of sulfur-containing smoke gas

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, and traditional water scrubber washing process is that flue gas gets into from the tower bottom, and washings get into from tower top; Contact with flue gas is reverse; Dust in flue gas is washed, get into 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 is developed in the 60-70 age in last century at first, is 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 (like 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 are prone to cause system jams on the equipment of being deposited on, pipeline and the desulfurizing tower internals, 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, said 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 gets into water.In order not allow the flue gas after the dedusting to 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, with circulation cleaning pump extraction 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, said step b is: the gas after step a handles with the desulfurizing agent desulfurization after gas-liquid separation be purified gas.

Said desulfurizing agent is at least a in aqueous solution of sodium bisulfite, the aqueous sodium carbonate.Rich solution pH value after the step b desulfurizing agent absorbing sulfur dioxide was directly used as desulfurizing agent in 5.6~6.0 o'clock.

Rich solution after the step b desulfurizing agent absorbing 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, filter gained filtrating and be 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, promptly get after the cooling.

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 deposition.If the solid impurity removal effect of filtrating is bad, can filter repeatedly 2~3 times.

The vacuum condition of step e concentrates through realizing that through 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 through the mother liquor pond, and the bottom of filter centrifugal is returned the pond through 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 vacuum extraction mouthful outflow from the vacuum concentration pot top, is condensed into condensate with condensate cooler, and condensate can be sent to obtain solution.

Step e receive crystal on contain adhesional wetting water, be transported to pneumatic drier with screw rod conveyor, the sodium sulfite after dehydrating is put export trade in storage through drying machine cooler cooling back packing.

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.Said 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, and 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 absorbed by desulfurizing agent, 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 the spray aqueous solution of sodium bisulfite at the desulfuration absorbing tower middle part, spray contains the aqueous solution of sodium hydrogensulfite and sodium carbonate on desulfuration absorbing tower top.Wherein aqueous sodium carbonate is fresh (being also referred to as lean solution), and aqueous solution of sodium bisulfite can fresh, also can use the solution (being also referred to as rich solution) after the aqueous sodium carbonate absorbing sulfur dioxide.Rich solution is extracted out by circulating pump at the bottom of desulfuration absorbing tower; Rich solution pH value can be used as the spray liquid inlet entering desulfuration absorbing tower of circulation desulfurization agent in the middle part of desulfuration absorbing tower and repeats to absorb the 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 is high; Dedusting, removal sulfur dioxide, depriving hydrogen sulphide efficient are up to 100%; Dust, sulfur dioxide equal size are zero in the flue; Can realize zero release of pollutant in the smoke evacuation,, can be used as the unstripped gas that industry and food-grade carbon-dioxide reclaim because the discharged gas fume depuration quality after this PROCESS FOR TREATMENT is very high;

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 possibly bring into of flue gas gets into circulation solution system, just possibly be deposited on filler, pipeline and the equipment wall, results in blockage, and can cause whole device parking when serious.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 solve other sulfur removal technology and the most often occurred the problem that the easy blocking device stops, fully assurance device long period even running at positions such as pipeline, wall, tower internals and fillers.

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 sketch map, 3 water scrubbers, 5 desulfuration absorbing towers.

Fig. 2 is the flue gas desulfurization technique sketch map, 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, and 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 bolognian stone (barium sulfate) and celestine (strontium sulfate) high temperature reduction rotary kiln sulfur-containing smoke gas; Before carrying out desulfurizing and purifying, need preparatory 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 is as shown in Figure 2

Sulfur-containing smoke gas gets into from water scrubber 3 lower ends, and the cavity of water from 3 two sections fillers of water scrubber gets into, and sulfur-containing smoke gas obtains removing the flue gas behind the dust through the washing section packing layer, the filler through 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 gets into 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 the desulfurizing agent absorbing 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 repeated to absorb the sulfur dioxide the sulfurous gas as the circulation desulfurization agent from the spray liquid inlet entering desulfuration absorbing tower 5 at desulfuration absorbing tower 5 middle parts.

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; Bolognian stone 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 bolognian stone 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 the 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 through the magnitude of recruitment of cooling water in the cat head chilled water unit.Water scrubber 3 bottom liquid level height can be through 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 through 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, filtering gained filtrating 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 after dehydrating is packing after the cooling of drying machine cooler, the warehouse-in export trade.

Vacuum condition concentrates down and realizes that through 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 through mother liquor pond 15, and the bottom of filter centrifugal 14 is returned pond 18 through 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 with vapor recycle water condensation cooler 11; The gas that is mixed with condensate divides flow container 16 separatory through vacuum buffer, receive condensate to be stored in vavuum pump circulation water pot 17 for use, can send to obtain solution.

Rich solution pH value is 5.6~6.0, reaches at 10.0 o'clock in neutralizing tank 7 adjustment pH values, 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 in solution, taked the measure of some anti-oxidation, sulphite is become the situation of sulfate to be difficult to avoid by dioxygen oxidation.According to commercial production, if do not remove sodium sulphate, the content of sodium sulphate is generally up to 5~6% (quality) in the anhydrous sodium sulfite of then producing.In order to reduce sodium sulphate content, need take off adding sulfate radical chemical agent to remove sulfate radical in neutralization stage.Iron content like fruit product is higher, or during frowziness, can after neutralization, add an amount of iron removing reagent and acticarbons such as vulcanized sodium, 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 like Fig. 2, shown in 3.

1, the preparatory 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 following:

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, 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 following:

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 be according to concrete flue gas compositing characteristic, through Lectotype and calculation.

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

Send the concentration of centrifugal 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 (5)

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, said sulfur-containing smoke gas dust content is 50~200mg/Nm 3, the middle part of desulfuration absorbing tower or top all can spray desulfurizing agent, and desulfurizing agent is an aqueous sodium carbonate;
Wherein, said 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; 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;
Said desulfuration absorbing tower comprises tower body, and 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; 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.
2. the integrated conduct method of sulfur-containing smoke gas according to claim 1, it is characterized in that: said 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 1 and 2 is characterized in that: receive after the washing of step a sulfur-containing smoke gas the washings solids removed by filtration particle that contains dust after, use as washings.
4. the integrated conduct method of sulfur-containing smoke gas according to claim 2, it is characterized in that: the rich solution pH value after the step b desulfurizing agent absorbing sulfur dioxide was directly used as desulfurizing agent in 5.6~6.0 o'clock.
5. the integrated conduct method of sulfur-containing smoke gas according to claim 2, it is characterized in that: the rich solution after the step b desulfurizing agent absorbing 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, filter gained filtrating and be 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, promptly get after the cooling.
CN2009103059928A 2009-08-24 2009-08-24 Comprehensive treatment method of sulfur-containing flue gas CN101637685B (en)

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