CN106268173A - A kind of method of flue gas desulfurization - Google Patents
A kind of method of flue gas desulfurization Download PDFInfo
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- CN106268173A CN106268173A CN201610769402.7A CN201610769402A CN106268173A CN 106268173 A CN106268173 A CN 106268173A CN 201610769402 A CN201610769402 A CN 201610769402A CN 106268173 A CN106268173 A CN 106268173A
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
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- B01D—SEPARATION
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
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- B01D2251/304—Alkali metal compounds of sodium
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- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
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- B01D2251/608—Sulfates
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- B01D2252/20—Organic absorbents
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- B01D2253/10—Inorganic adsorbents
- B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
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Abstract
A kind of method that the invention discloses flue gas desulfurization, including: flue gas is passed sequentially through the first desulfurizing tower, the second desulfurizing tower and the 3rd desulfurizing tower and carries out desulfurization；Desulfurizing agent in described first desulfurizing tower is organic amine desulfurizer；The solid desulfurating agent that aperture is 0.4～3nm it is provided with in described second desulfurizing tower；Desulfurizing agent in described 3rd desulfurizing tower is akaline liquid desulfurizing agent.Solid desulfurating agent, akaline liquid desulfurizing agent that the present invention uses organic amine desulfurizer, aperture to be 0.4～3nm carry out desulfurization process to flue gas successively, so that SO in the gas that the 3rd desulfurizing tower is out2Meet GB13271 2001 national standard and GB13223 2011 national standard.Test result indicate that, the method for flue gas desulfurization of the present invention, desulfuration efficiency is more than 97.5%.
Description
Technical field
The present invention relates to flue gas desulfurization field, a kind of method particularly relating to flue gas desulfurization.
Background technology
Sulfur dioxide is a kind of toxic gas, is easily soluble in blood and other stickiness liquid of human body, has human body greatly
Injury.Research shows, under the influence of the sulfur dioxide of high concentration, plant leaf blade surface produces ecthyma gangrenosa, or directly makes plant
Blade is withered to come off；Under the influence of low-concentration sulfur dioxide, the GF of plant is affected, and causes yield to decline.And
And sulfur dioxide has corrosiveness to metal, bring the biggest loss to national economy every year.According to estimates, industrially developed country is every
Year is because the direct economic loss that metal erosion brings accounts for the 2%～4% of total value of production in national economy.From the foregoing, titanium dioxide
Sulfur causes the biggest impact to industrial or agricultural, crowd, and country is more and more higher to administering sulfur dioxide attention rate, administers containing dioxy
The flue gas changing sulfur is very urgent.
Flue gas desulfurization refers to remove sulfur oxygen the flue gas produced when the combustion of fossil fuel such as coal or other industrial waste gases
Compound, is the maximally efficient He main technological means of control of acid rain and sulfur dioxide pollution.At present, countries in the world are to flue gas
Desulfurization technology is all paid much attention to, and has been developed for tens of kinds of effective flue gas desulfurization techniques, and its ultimate principle is all with basic species
Matter is as the absorbent of oxysulfide, i.e. desulfurizing agent.
Limestone scrubbing FGD is current Application comparison fume desulphurization method widely the most in the world, uses Calx masonry
For desulfurizing agent, this technique history of existing 50 years, after continuously improving and improving, Technical comparing is ripe, and has
Desulfuration efficiency is high, and unit capacity is big, and coal adaptability is strong and the advantage such as side-product easily recovery.The thermal power plant of China, steel mill, 90%
More than use limestone scrubbing FGD flue gas desulfurization process, but the desulfuration efficiency of said method is low.
Summary of the invention
In view of this, a kind of method that the invention provides flue gas desulfurization, the method can improve desulfuration efficiency.
The technical scheme is that and be achieved in that:
A kind of method of flue gas desulfurization, including:
Flue gas is passed sequentially through the first desulfurizing tower, the second desulfurizing tower and the 3rd desulfurizing tower and carries out desulfurization；
Desulfurizing agent in described first desulfurizing tower is organic amine desulfurizer；
The solid desulfurating agent that aperture is 0.4～3nm it is provided with in described second desulfurizing tower；
Desulfurizing agent in described 3rd desulfurizing tower is akaline liquid desulfurizing agent.
Preferably, described organic amine desulfurizer is in monomethylaniline., monoethanolamine, diethanolamine and triethanolamine
One or more.
Preferably, one or more in activated carbon, limestone, ferrum oxide of described solid desulfurating agent.
Preferably, described akaline liquid desulfurizing agent is sodium hydroxide solution, sodium carbonate liquor, calcium silicate slag solution or alkalescence sulfur
Acid aluminum solutions.
Preferably, described akaline liquid desulfurizing agent neutral and alkali material is 3～10:1 with the mass ratio of water.
Preferably, in described first desulfurizing tower, the flow of flue gas is 1000～1800m3/ h, described organic amine desulfurizer
Flow be 30～80m3/h。
Preferably, between described first desulfurizing tower and described second desulfurizing tower, described second desulfurizing tower takes off with the described 3rd
It is provided with air accumulator between sulfur tower.
Preferably, in described second desulfurizing tower, the flow of flue gas is 110～190m3/ h, described solid desulfurating agent is changed secondary
Number is 2～5 times/h.
Preferably, in described 3rd desulfurizing tower, the flow of flue gas is 50～80m3/ h, the stream of described akaline liquid desulfurizing agent
Amount is 3～8m3/h。
The invention have the benefit that
A kind of method of flue gas desulfurization that the present invention provides, using organic amine desulfurizer, aperture is 0.4～3nm consolidate
Body desulfurizing agent, akaline liquid desulfurizing agent carry out desulfurization process to flue gas successively, so that in the gas that the 3rd desulfurizing tower is out
SO2Meet GB13271-2001 national standard and GB13223-2011 national standard.Test result indicate that, gaseous contamination of the present invention
The method of thing, desulfuration efficiency is more than 97.5%.
Detailed description of the invention
A kind of method that the invention discloses flue gas desulfurization, those skilled in the art can use for reference present disclosure, suitably change
Enter technological parameter to realize.Special needs to be pointed out is, described similar replacement and change are aobvious for a person skilled in the art
And be clear to, they are considered as being included in the present invention.The method of the present invention and quoting is carried out by preferred embodiment
Describing, method described herein and application substantially can be carried out in without departing from present invention, spirit and scope by related personnel
Change or suitably change and combination, realize and apply the technology of the present invention.
The method of a kind of flue gas desulfurization that the present invention provides, including:
Flue gas is passed sequentially through the first desulfurizing tower, the second desulfurizing tower and the 3rd desulfurizing tower and carries out desulfurization；
Desulfurizing agent in first desulfurizing tower is organic amine desulfurizer；
The solid desulfurating agent that aperture is 0.4～3nm it is provided with in second desulfurizing tower；
Desulfurizing agent in 3rd desulfurizing tower is akaline liquid desulfurizing agent.
In the present invention, organic amine desulfurizer can be by flue gas 75～the SO of 85%2Slough；And organic amine desulfurization
Agent can not only absorb SO2, but also SO can be separated out2, it is simple to SO2Application at other field；Aperture is 0.4～3nm consolidates
Body desulfurizing agent can adsorb the first desulfurizing tower flue gas out further；Akaline liquid desulfurizing agent can by the second desulfurizing tower out
Flue gas carry out advanced treating so that in the 3rd desulfurizing tower gas out sulfur content meet GB13271-2001 national standard and
GB13223-2011 national standard.
Test result indicate that, the method for flue gas desulfurization of the present invention, desulfuration efficiency is more than 97.5%.
In the present invention, organic amine desulfurizer, and can be more than predetermined temperature at predetermined temperature sulfur dioxide absorption
Temperature separate out sulfur dioxide, predetermined temperature such as in the range of 30～50 DEG C, desulfurizing agent separate out sulfur dioxide temperature can
With at 60 DEG C.In an embodiment of the present invention, organic amine desulfurizer is selected from monomethylaniline., monoethanolamine, diethanolamine and three
One or more in ethanolamine；In other embodiments of the invention, organic amine desulfurizer is selected from monomethylaniline., an ethanol
One or both in amine, diethanolamine and triethanolamine.
In an embodiment of the present invention, the first desulfurizing tower desulfurization temperature is 50～80 DEG C.
In an embodiment of the present invention, in the first desulfurizing tower, the flow of flue gas is 1000～1800m3/ h, organic amine takes off
The flow of sulfur agent is 30～80m3/h；In other embodiments of the invention, in the first desulfurizing tower the flow of flue gas be 1200～
1500m3/ h, the flow of organic amine desulfurizer is 50～60m3/h。
In an embodiment of the present invention, between the first desulfurizing tower and the second desulfurizing tower, the second desulfurizing tower and the 3rd desulfurizing tower
It is provided with air accumulator.
In the present invention, the solid desulfurating agent of 0.4～3nm for the further desulfurization of gas out of the first desulfurizing tower,
And the desulfurization degree of the solid desulfurating agent in this aperture is high.In an embodiment of the present invention, solid desulfurating agent is selected from activated carbon, Calx
One or more in stone, ferrum oxide；In other embodiments of the invention, solid desulfurating agent be selected from activated carbon, limestone,
One or both in ferrum oxide.
In an embodiment of the present invention, in the second desulfurizing tower, the flow of flue gas is 110～190m3/ h, solid desulfurating agent is more
Changing number of times is 2～5 times/h；In other embodiments of the invention, in the second desulfurizing tower, the flow of flue gas is 130～160m3/ h,
It is 3～4 times/h that solid desulfurating agent changes number of times.
In an embodiment of the present invention, the desulfurization temperature of the second desulfurizing tower is 30～50 DEG C.
In an embodiment of the present invention, solid desulfurating agent is the solid desulfurating agent of dipping parlkaline solution；The present invention's
In other embodiments, alkaline solution is sodium hydroxide, calcium hydroxide or sodium carbonate.
In the present invention, akaline liquid desulfurizing agent can process the second desulfurizing tower out flue gas further.The present invention's
In embodiment, akaline liquid desulfurizing agent is sodium hydroxide solution, sodium carbonate liquor, calcium silicate slag solution or basic sulfate aluminum solutions；
In other embodiments of the invention, akaline liquid desulfurizing agent is sodium hydroxide solution or calcium silicate slag solution；Another in the present invention
In outer embodiment, akaline liquid desulfurizing agent is calcium silicate slag solution.
In an embodiment of the present invention, alkaline solution desulfurizing agent neutral and alkali material is 3～10:1 with the mass ratio of water.
Wherein, the composition in calcium silicate slag solution is dicalcium silicate 25～45%, hydratable calcium pyralspite 30～45%, calcite
10～15% and aluminate hydrates DFP 5～12%.The calcium silicate slag of mentioned component, as desulfurizing agent, can not only effectively realize flue gas and take off
Sulfur, moreover it is possible to calcium silicate slag is carried out twice laid, it is to avoid its discharge pollution to soil and groundwater.
In an embodiment of the present invention, the desulfurization temperature of the 3rd desulfurizing tower is 80～120 DEG C.
In an embodiment of the present invention, in the 3rd desulfurizing tower, the flow of flue gas is 50～80m3/ h, akaline liquid desulfurizing agent
Flow be 3～8m3/h
In order to further illustrate the present invention, below in conjunction with embodiment, the method for the flue gas desulfurization that the present invention provides is carried out in detail
Thin description.
Embodiment 1
Flue gas is first passed through the first desulfurizing tower, and the desulfurizing agent in the first desulfurizing tower is monomethylaniline., and desulfurization temperature is 60 DEG C,
The flow of flue gas is 1000m3/ h, the flow of monomethylaniline. is 30m3/h；And the flue gas after processing is stored in air accumulator.Will
Flue gas in air accumulator is passed through the second desulfurizing tower, is provided with the activated carbon that aperture is 1.5nm in the second desulfurizing tower, and desulfurization temperature is
30 DEG C, flue gas flow is 110m3/ h, the flue gas after the replacing number of times of activated carbon is 2 times/h and will process is stored in air accumulator.
Finally the gas processed in pipe being passed through the 3rd desulfurizing tower, the desulfurizing agent in the 3rd desulfurizing tower is sodium hydroxide solution, hydroxide
In sodium solution, sodium hydroxide is 3:1 with the mass ratio of water, and desulfurization temperature is 80 DEG C, and flue gas flow is 50m3/ h, sodium hydroxide is molten
The flow of liquid is 3m3/h。
After testing, SO in flue gas is carried out before desulfurization2Concentration is 3102mg/Nm3, SO in flue gas after desulfurization2Concentration is 77mg/
Nm3, desulfuration efficiency is 97.5%.
Embodiment 2
Flue gas is first passed through the first desulfurizing tower, and the desulfurizing agent in the first desulfurizing tower is monoethanolamine, and desulfurization temperature is 50 DEG C,
The flow of flue gas is 1300m3/ h, the flow of monoethanolamine is 80m3/h；And the flue gas after processing is stored in air accumulator.Will
Flue gas in air accumulator is passed through the second desulfurizing tower, is provided with the limestone that aperture is 0.8nm in the second desulfurizing tower, and desulfurization temperature is
50 DEG C, flue gas flow is 145m3/ h, the flue gas after the replacing number of times of limestone is 3 times/h and will process is stored in air accumulator.
Finally the gas processed in pipe being passed through the 3rd desulfurizing tower, the desulfurizing agent in the 3rd desulfurizing tower is sodium carbonate liquor, and sodium carbonate is molten
In liquid, sodium carbonate is 6:1 with the mass ratio of water, and desulfurization temperature is 100 DEG C, and flue gas flow is 60m3/ h, the flow of sodium carbonate liquor
For 3m3/h。
After testing, SO in flue gas is carried out before desulfurization2Concentration is 3102mg/Nm3, SO in flue gas after desulfurization2Concentration is 71mg/
Nm3, desulfuration efficiency is 97.7%.
Embodiment 3
Flue gas is first passed through the first desulfurizing tower, and the desulfurizing agent in the first desulfurizing tower is monoethanolamine and diethanolamine, desulfurization
Temperature is 80 DEG C, and the flow of flue gas is 1500m3The flow of/h, monoethanolamine and diethanolamine is 50m3/h；And after processing
Flue gas is stored in air accumulator.Flue gas in air accumulator is passed through the second desulfurizing tower, and being provided with aperture in the second desulfurizing tower is 1nm
Activated carbon and ferrum oxide, desulfurization temperature is 40 DEG C, and flue gas flow is 160m3The replacing number of times of/h, activated carbon and ferrum oxide is 4
Secondary/h and will process after flue gas be stored in air accumulator.The gas processed in pipe is finally passed through the 3rd desulfurizing tower, and the 3rd takes off
Desulfurizing agent in sulfur tower is basic sulfate aluminum solutions, and basic sulfate aluminum solutions neutral and alkali aluminum sulfate is 5:1 with the mass ratio of water, de-
Sulfur temperature is 90 DEG C, and flue gas flow is 70m3/ h, the flow of basic sulfate aluminum solutions is 3m3/h。
After testing, SO in flue gas is carried out before desulfurization2Concentration is 3102mg/Nm3, SO in flue gas after desulfurization2Concentration is 52mg/
Nm3, desulfuration efficiency is 98.3%.
Embodiment 4
Flue gas is first passed through the first desulfurizing tower, and the desulfurizing agent in the first desulfurizing tower is diethanolamine and triethanolamine, desulfurization
Temperature is 70 DEG C, and the flow of flue gas is 1200m3The flow of/h, diethanolamine and triethanolamine is 60m3/h；And after processing
Flue gas is stored in air accumulator.Flue gas in air accumulator is passed through the second desulfurizing tower, and being provided with aperture in the second desulfurizing tower is 3nm
Activated carbon and limestone, desulfurization temperature is 35 DEG C, and flue gas flow is 130m3The replacing number of times of/h, activated carbon and limestone is 3
Secondary/h and will process after flue gas be stored in air accumulator.The gas processed in pipe is finally passed through the 3rd desulfurizing tower, and the 3rd takes off
Desulfurizing agent in sulfur tower is calcium silicate slag solution, and in calcium silicate slag solution, calcium silicate slag is 7:1 with the mass ratio of water, and desulfurization temperature is 100
DEG C, flue gas flow is 60m3/ h, the flow of calcium silicate slag is 3m3/h。
After testing, SO in flue gas is carried out before desulfurization2Concentration is 3102mg/Nm3, SO in flue gas after desulfurization2Concentration is 58mg/
Nm3, desulfuration efficiency is 98.1%.
Embodiment 5
Flue gas is first passed through the first desulfurizing tower, and the desulfurizing agent in the first desulfurizing tower is monomethylaniline. and triethanolamine, desulfurization
Temperature is 65 DEG C, and the flow of flue gas is 1800m3The flow of/h, monomethylaniline. and triethanolamine is 55m3/h；And after processing
Flue gas is stored in air accumulator.Flue gas in air accumulator is passed through the second desulfurizing tower, and being provided with aperture in the second desulfurizing tower is
The limestone of 0.4nm and ferrum oxide, desulfurization temperature is 45 DEG C, and flue gas flow is 190m3The replacing of/h, limestone and ferrum oxide time
Flue gas after number is 5 times/h and will process is stored in air accumulator.Finally the gas processed in pipe is passed through the 3rd desulfurizing tower, the
Desulfurizing agent in three desulfurizing towers is sodium carbonate liquor, and in sodium carbonate liquor, sodium carbonate is 10:1 with the mass ratio of water, desulfurization temperature
Being 120 DEG C, flue gas flow is 50m3/ h, the flow of sodium carbonate liquor is 3m3/h。
After testing, SO in flue gas is carried out before desulfurization2Concentration is 3102mg/Nm3, SO in flue gas after desulfurization2Concentration is 64mg/
Nm3, desulfuration efficiency is 97.9%.
The foregoing is only presently preferred embodiments of the present invention, not in order to limit the present invention, all essences in the present invention
Within god and principle, any modification, equivalent substitution and improvement etc. made, should be included within the scope of the present invention.
Claims (9)
1. the method for a flue gas desulfurization, it is characterised in that including:
Flue gas is passed sequentially through the first desulfurizing tower, the second desulfurizing tower and the 3rd desulfurizing tower and carries out desulfurization；
Desulfurizing agent in described first desulfurizing tower is organic amine desulfurizer；
The solid desulfurating agent that aperture is 0.4～3nm it is provided with in described second desulfurizing tower；
Desulfurizing agent in described 3rd desulfurizing tower is akaline liquid desulfurizing agent.
2. the method for claim 1, it is characterised in that described organic amine desulfurizer is selected from monomethylaniline., an ethanol
One or more in amine, diethanolamine and triethanolamine.
3. the method for claim 1, it is characterised in that described solid desulfurating agent is selected from activated carbon, limestone, ferrum oxide
In one or more.
4. the method for claim 1, it is characterised in that described akaline liquid desulfurizing agent is sodium hydroxide solution, carbonic acid
Sodium solution, calcium silicate slag solution or basic sulfate aluminum solutions.
5. method as claimed in claim 4, it is characterised in that described akaline liquid desulfurizing agent neutral and alkali material and the quality of water
Ratio is 3～10:1.
6. the method for claim 1, it is characterised in that in described first desulfurizing tower the flow of flue gas be 1000～
1800m3/ h, the flow of described organic amine desulfurizer is 30～80m3/h。
7. the method for claim 1, it is characterised in that between described first desulfurizing tower and described second desulfurizing tower, institute
State and be provided with air accumulator between the second desulfurizing tower and described 3rd desulfurizing tower.
8. the method for claim 1, it is characterised in that in described second desulfurizing tower, the flow of flue gas is 110～190m3/
H, it is 2～5 times/h that described solid desulfurating agent changes number of times.
9. the method for claim 1, it is characterised in that in described 3rd desulfurizing tower, the flow of flue gas is 50～80m3/ h,
The flow of described akaline liquid desulfurizing agent is 3～8m3/h。
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| CN201610769402.7A CN106268173A (en) | 2016-08-29 | 2016-08-29 | A kind of method of flue gas desulfurization |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN115445420A (en) * | 2022-07-07 | 2022-12-09 | 南京永能新材料有限公司 | Cement kiln flue gas liquid desulfurizer and preparation method thereof |
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| CN113058410A (en) * | 2021-03-19 | 2021-07-02 | 浙江大江节能科技有限公司 | Desulfurizing agent for glass kiln flue gas and preparation method thereof |
| CN115445420A (en) * | 2022-07-07 | 2022-12-09 | 南京永能新材料有限公司 | Cement kiln flue gas liquid desulfurizer and preparation method thereof |
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