CN107042062A - Gas sweetening method of denitration - Google Patents
Gas sweetening method of denitration Download PDFInfo
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- CN107042062A CN107042062A CN201710185064.7A CN201710185064A CN107042062A CN 107042062 A CN107042062 A CN 107042062A CN 201710185064 A CN201710185064 A CN 201710185064A CN 107042062 A CN107042062 A CN 107042062A
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- 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
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
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Abstract
The invention discloses a kind of gas sweetening method of denitration, to solve synchronously carry out the technical problem of desulphurization denitration in the prior art.The gas sweetening method of denitration includes procedure below：Sulfur dioxide and nitrogen oxides in I, gases are absorbed and are oxidized to corresponding acid ion respectively to generate corresponding acid in first absorbing liquid by the first absorbing liquid containing oxidant simultaneously；Acid described in II, reacts and generation and the corresponding salt of the acid ion respectively with entering the first alkaline matter in the first absorbing liquid respectively；III, reclaims described salt.This method can solve the problem that can not synchronously carry out the technical problem of desulphurization denitration in the prior art, the purified treatment for fiery (heat) the electric industry coal-fired flue-gas such as industry and steel oil that is particularly suitable for use in.
Description
Technical field
The present invention relates to gas sweetening denitration technology field, in particular to gas sweetening method of denitration, gas sweetening
Denitrating system and the flue gas purification system for applying the gas sweetening denitrating system.
Background technology
The technology category of existing flue gas desulfurization (Flue gas desulfurization, abbreviation FGD) technology mainly has
Gypsum, spray drying process, phospho-ammonium fertilizer method, in-furnace calcium spraying afterbody humidification method, flue gas circulating fluidized bed method, electronic beam method and ammonia
Water washing method etc..Wherein, gypsum technique is technology most commonly used in the world, and proportion is more than 90%.
The principle of gypsum technique is：Agstone is added water slurries are made to be pumped into absorption tower as absorbent and filled with flue gas
Tap touches the SO in mixing, flue gas2The air blasted with the calcium carbonate in slurries and from tower bottom carries out oxidation reaction generation
Calcium sulfate and after certain saturation degree is reached crystallization form dihydrate gypsum, the gypsum slurries discharged through absorption tower are concentrated, dehydration,
Then the stacking of gypsum bunker is delivered to conveyer, the flue gas after desulfurization is discharged into air after demisting and heat temperature raising by chimney.
The main selective noncatalytic reduction (SNCR) of the technology category of existing gas denitrifying technology and selectivity are urged
Change reducing process (SCR).Wherein, selective catalytic reduction is most ripe gas denitrifying technology at present, and its principle is by also
Former agent (NH3Or urea) under metallic catalyst effect, optionally with NOXReaction generation N2And H2O。
For containing SO simultaneously2And NOXGas, the industry coal-fired flue-gas such as fiery (heat) electric industry and steel oil shows
Distribution carries out desulfurization and denitration after above-mentioned flue gas desulfurization technique and flue-gas denitration process can only be combined by the stage, not only work
Skill system is complicated, cost is high, while administering not thorough to the harmful components in gas, especially for greenhouse gases CO2It is exceeded
Emission problem is not solved effectively.
The content of the invention
It is a primary object of the present invention to provide a kind of gas sweetening method of denitration, gas sweetening denitrating system and application
The flue gas purification system of the gas sweetening denitrating system, to solve synchronously carry out the technology of desulphurization denitration in the prior art
Problem.
To achieve these goals, according to an aspect of the invention, there is provided a kind of gas sweetening method of denitration.The gas
Body desulfurization denitration method includes procedure below：Sulfur dioxide and nitrogen oxides in I, gases are simultaneously by first containing oxidant
Absorbing liquid absorbs and is oxidized to corresponding acid ion respectively to generate corresponding acid in first absorbing liquid；Ⅱ.
Described acid into the first alkaline matter in the first absorbing liquid respectively with reacting and generating and the acid ion respectively
Corresponding salt；III, reclaims described salt.
In the above method, the process I can be made to occur in first reactor, process II occurs in second reactor；
At this moment, it should be connected to transmit between the first reactor and second reactor by the first absorbing liquid after the process I
The passage of the recovered liquid of transformation, the second reactor should be connected to deliver first alkalescence into second reactor
The alkali source feedway of material.By such setting, be conducive to as desired by deliver the first different alkaline matters from
And different salt are obtained in second reactor.
The process I can also be made to occur in same reactor with process II；At this moment, used in the process I
The first absorbing liquid in should not only containing the oxidant simultaneously again contain first alkaline matter., can by such setting
To shorten the convergence time between process I and process II, to reach higher operating efficiency.
Further, sulfur dioxide and nitrogen oxides are oxidized to sulfate ion and nitrate anion respectively in the process I
Ion is so as to generation sulfuric acid and nitric acid in the first absorbing liquid；In the process II sulfuric acid and nitric acid respectively with the first basic species
Matter reacts and generates sulfate and nitrate respectively.By such setting, result in widely used sulfate and
Nitrate, therefore bring higher economic benefit.
Further, the oxidant selected from hydrogen peroxide, with the process II in the first alkaline matter metal sun from
Son is any one or a few in the Peroxides and Superoxides of same metal.By such setting, oxidant makes
With will not introduce not tractable impurity, and these oxidants are easily obtained, are easy to cost control.
Further, first alkaline matter is selected from ammonia, ammonium carbonate, ammonium hydrogen carbonate, calcium hydroxide, calcium oxide, carbonic acid
In calcium, calcium bicarbonate, potassium hydroxide, potassium carbonate, saleratus, sodium hydroxide, sodium carbonate, sodium acid carbonate any one or it is several
Kind.The more suitable present invention of the first above-mentioned alkaline matter, therefore be currently preferred first alkaline matter.
Further, the above method also includes the process IV that need not be carried out after the process II or process III：Will not
The tail gas containing carbon dioxide absorbed by first absorbing liquid is inhaled with the second absorbing liquid containing the second alkaline matter
Receive to be carbonate and/or bicarbonate by the carbon dioxide conversion.Pass through such setting, additionally it is possible to remove in tail gas
Carbon dioxide, reduce carbon emission, and useful carbonate and/or bicarbonate can be obtained.
Further, second alkaline matter is any one in ammonia, calcium hydroxide, potassium hydroxide, sodium hydroxide
Plant or several.The more suitable present invention of the second above-mentioned alkaline matter, therefore be currently preferred second alkaline matter.
Further, the bicarbonate that can also generate second alkaline matter and the carbon dioxide reaction is used as the
One alkaline matter is back to the process II.It can be seen from content above, the preferable ammonium hydrogen carbonate of the first alkaline matter, carbonic acid
Hydrogen calcium, saleratus or sodium acid carbonate, when the second alkaline matter is preferably ammonia, calcium hydroxide, potassium hydroxide or sodium hydroxide,
At this moment, process IV can be generated by the correspondence generation of process IV ammonium hydrogen carbonate, calcium bicarbonate, saleratus or sodium acid carbonate
Ammonium hydrogen carbonate, calcium bicarbonate, saleratus or sodium acid carbonate are back to the process II as the first alkaline matter, both alleviate
The difficulty for the bicarbonate that processing procedure IV is generated, is also beneficial to save the consumption of the first alkaline matter.
Further, the above method also includes the pretreatment that dedusting is carried out to the gas that will enter the process I
Process.By such setting, more pure product (i.e. various salt) can be obtained by process II and subsequent process, together
When be also beneficial to reduce dust emission.
To achieve these goals, there is provided a kind of gas sweetening denitrating system according to another aspect of the present invention.Should
Gas sweetening denitrating system is used to handle the gas containing sulfur dioxide and nitrogen oxides, and it includes：First reactor, described
One reactor absorbs the sulfur dioxide and nitrogen oxides in the gas using the first absorbing liquid containing oxidant and will simultaneously
They are oxidized to corresponding acid ion to obtain corresponding acid in the recovered liquid that the first absorbing liquid changes respectively；The
Two reactors, the second reactor is reacted using the first alkaline matter and described acid and generated and the acid group respectively
The corresponding salt of ion；Wherein, it is connected between the first reactor and second reactor for transmitting the recovered liquid
Passage, the alkali source that the second reactor is connected with for delivering first alkaline matter into second reactor supplies dress
Put.
Further, the first reactor uses spray absorber, is sprayed when the spray absorber works to the gas
Drench the first absorbing liquid and be recycled liquid in bottom of towe.Spray absorber is that chemical industry is common absorbs gas by absorbing liquid
And the equipment for obtaining corresponding product, suitably as the first reactor of the present invention.
Further, the second reactor uses the reactor with stirring structure.Reactor is equally chemical industry
Common equipment, and suitably as the second reactor of the present invention.
Further, the first reactor is absorbed in the gas simultaneously using the first absorbing liquid containing oxidant
They simultaneously are oxidized to sulfate ion and nitrate ion in the first absorbing liquid to turn by sulfur dioxide and nitrogen oxides respectively
Sulfuric acid and nitric acid are obtained in the recovered liquid become；The second reactor uses the first alkaline matter and the sulfuric acid and nitric acid
React and generate sulfate and nitrate respectively.By such setting, widely used sulfate and nitre is resulted in
Hydrochlorate, therefore bring higher economic benefit.
Further, it is gold of the same race that the oxidant, which is selected from hydrogen peroxide and the metal cation of first alkaline matter,
Any one or a few in the Peroxides and Superoxides of category.By such setting, the use of oxidant will not be introduced
Not tractable impurity, and these oxidants are easily obtained, are easy to cost control.
Further, first alkaline matter is selected from ammonia, ammonium carbonate, ammonium hydrogen carbonate, calcium hydroxide, calcium oxide, carbonic acid
In calcium, calcium bicarbonate, potassium hydroxide, potassium carbonate, saleratus, sodium hydroxide, sodium carbonate, sodium acid carbonate any one or it is several
Kind.The more suitable present invention of the first above-mentioned alkaline matter, therefore be currently preferred first alkaline matter.
Further, including the 3rd reactor, the 3rd reactor is used to receive and not inhaled by first absorbing liquid
Receive the tail gas containing carbon dioxide and with by the tail gas is carried out with the second absorbing liquid containing the second alkaline matter absorb so that
It is carbonate and/or bicarbonate by the carbon dioxide conversion.Pass through such setting, additionally it is possible to remove the dioxy in tail gas
Change carbon, reduce carbon emission, and useful carbonate and/or bicarbonate can be obtained.
Further, second alkaline matter is any one in ammonia, calcium hydroxide, potassium hydroxide, sodium hydroxide
Plant or several.The more suitable present invention of the second above-mentioned alkaline matter, therefore be currently preferred second alkaline matter.
Further, be connected between the 3rd reactor and second reactor for will second alkaline matter and
The bicarbonate of the carbon dioxide reaction generation flows back in the conveyer of second reactor as the first alkaline matter.According to
Knowable to content above, the preferable ammonium hydrogen carbonate of the first alkaline matter, calcium bicarbonate, saleratus or sodium acid carbonate, when second
When alkaline matter is preferably ammonia, calcium hydroxide, potassium hydroxide or sodium hydroxide, can by process IV correspondence generation ammonium hydrogen carbonate,
Calcium bicarbonate, saleratus or sodium acid carbonate, at this moment, the ammonium hydrogen carbonate that is generated process IV by conveyer, calcium bicarbonate,
Saleratus or sodium acid carbonate are back to the process II as the first alkaline matter, have both alleviated the carbon of the generation of processing procedure IV
The difficulty of sour hydrogen salt, is also beneficial to save the consumption of the first alkaline matter.
To achieve these goals, there is provided a kind of flue gas purification system according to a further aspect of the invention.The flue gas
The blower fan that cleaning system includes gas dust remover, is connected with the gas exhaust port of dedusting of gas dust remover, is removed in the gas
Any one above-mentioned gas sweetening denitrating system is connected between dirt device and blower fan.
The above-mentioned gas desulfurization denitration method of the present invention, gas sweetening denitrating system and apply the gas sweetening denitration
The flue gas purification system of system can solve the problem that can not synchronously carry out the technical problem of desulphurization denitration in the prior art, be particularly suitable for use in
The purified treatment of fiery (heat) electric industry coal-fired flue-gas such as industry and steel oil.
The present invention is described further with reference to the accompanying drawings and detailed description.The additional aspect of the present invention and excellent
Point will be set forth in part in the description, and partly will become apparent from the description below, or pass through the practice of the present invention
Solve.
Brief description of the drawings
Constitute the part of the present invention accompanying drawing be used for aiding in content provided in the understanding of the present invention, accompanying drawing and its
Explanation relevant in the present invention can be used for explaining the present invention, but not constitute inappropriate limitation of the present invention.In the accompanying drawings：
Fig. 1 is the schematic diagram of a kind of gas sweetening denitrating system of the invention and the flue gas purification system using the system.
Fig. 2 is the schematic diagram of a kind of gas sweetening denitrating system of the invention and the flue gas purification system using the system.
Embodiment
Clear, complete explanation is carried out to the present invention below in conjunction with the accompanying drawings.Those of ordinary skill in the art are based on these
It is possible to realize the present invention in the case of explanation.Before with reference to accompanying drawing, the present invention will be described, it is necessary to it is emphasized that：
(1) in the technical scheme and technical characteristic provided in each several part including the description below in the present invention,
In the case of not conflicting, these technical schemes and technical characteristic can be mutually combined.
(2) embodiments of the invention being related in the description below are generally only the embodiment of a branch of the invention, without
It is whole embodiments.Therefore, based on the embodiment in the present invention, those of ordinary skill in the art are not making creative labor
The every other embodiment obtained on the premise of dynamic, should all belong to the scope of protection of the invention.
(3) on the explanation to term in the present invention.In description and claims of this specification and relevant part
Term " first ", " second " etc. be easily to cause the object confused for distinguishing, without for describe specific order or
Precedence.In addition, term " comprising " and " having " and their any deformation, it is intended that covering is non-exclusive to be included.
The signal of a kind of gas sweetening denitrating systems of the Fig. 1 for the present invention and the flue gas purification system using the system
Figure.As shown in figure 1, the flue gas purification system of the embodiment includes gas dust remover 100, the gas sweetening denitration system being sequentially connected
System 200, gas decarbonization system 300, blower fan 400 and tapping equipment 500.
Wherein, gas dust remover 100 can use mechanical dust collector (such as cyclone dust collectors), electric cleaner, bag-type dust
The combination of the cleaners such as device, metal filtering core deduster, ceramic filter-element dust collector or these cleaners.Be proposed with have compared with
Sack cleaner, metal filtering core deduster or the ceramic filter-element dust collector of high efficiency of dust collection, so that it is guaranteed that from gas dust remover 100
The gas exhaust port of dedusting discharge gas in dust content it is relatively low, be so conducive to the subsequent treatment to gas.
In the present embodiment, gas sweetening denitrating system 200 is actually one and absorbed by absorbing liquid in gas
Sulfur dioxide and nitrogen oxides and the reactor for obtaining corresponding product.Specifically, described reactor is spray absorber.Spray
It is the common equipment that gas is absorbed by absorbing liquid and corresponding product is obtained of chemical industry to drench absorption tower, with technology maturation
The advantages of spending high.Certainly, realize that the reactor of similar functions not only has spray absorber a kind of, the equipment such as reactor is also can
Capable selection.
For ease of description, the first suction will be referred to as absorbing liquid used in the reactor of gas sweetening denitrating system 200
Receive liquid 201.The key features of first absorbing liquid 201 are containing oxidant, therefore, when the sulfur dioxide in gas and nitrogen oxygen
Compound can be oxidized to corresponding acid ion respectively so as to raw in first absorbing liquid when being absorbed by the first absorbing liquid
Into corresponding acid；In addition, also containing the first alkaline matter in first absorbing liquid simultaneously, can occur respectively with described acid anti-
The salt corresponding with the acid ion and should be generated respectively.
For ease of description, by the sulfur dioxide and nitrogen oxides in gas simultaneously by the first absorbing liquid containing oxidant
201 absorb and are oxidized to corresponding acid ion respectively so as to which the process of the corresponding acid of generation in first absorbing liquid claims
For process I, the first alkaline matter is reacted with described acid respectively and generation and the acid ion are corresponding respectively
The process of salt is referred to as process II, then in the present embodiment, it is however generally that, sulfur dioxide and nitrogen oxides difference in the process I
Sulfate ion and nitrate ion is oxidized to generate sulfuric acid and nitric acid, the process II in the first absorbing liquid 201
In the sulfuric acid and nitric acid reacted respectively with the first alkaline matter and generate sulfate and nitrate respectively.
Obviously, the gas of spray absorber, the sulfate of generation are entered by the continuous circulated sprinkling of the first absorbing liquid 201
It will be progressively enriched with the bottom of spray absorber, finally reclaimed from the bottom of towe of spray absorber with nitrate.
In the present embodiment, gas decarbonization system 300 be the carbon dioxide that is absorbed by absorbing liquid in gas simultaneously
Obtain the reactor of corresponding product.Specifically, described reactor equally have selected spray absorber.
As gas decarbonization system 300 spray absorber pending gas inlet and be used as gas sweetening denitration system
The tail gas exhaust outlet connection of the spray absorber of system 200, therefore, the gas decarbonization system 300 is undertaken on gas sweetening denitration system
Further decarburization is carried out to the gas after desulphurization denitration is handled after system 200.
For ease of description, the second absorbing liquid will be referred to as absorbing liquid used in the reactor of gas decarbonization system 300
301.The key features of second absorbing liquid 301 are containing the second alkaline matter, therefore, when the carbon dioxide in gas is by
When two absorbing liquids 301 absorb, the second alkaline matter will generate carbonate and/or bicarbonate with the carbon dioxide reaction.
By the continuous circulated sprinkling of the second absorbing liquid 301 enter spray absorber gas, the carbonate of generation and/or
Bicarbonate will be progressively enriched with the bottom of spray absorber, is finally reclaimed from the bottom of towe of spray absorber.
Tail gas exhaust outlet as the spray absorber of gas decarbonization system 300 passes through the connection tapping equipment of blower fan 400
500.Therefore, the tail gas that gas decarbonization system 300 is discharged is discharged into air under the driving of blower fan 400 from tapping equipment 500.
It can be seen that, the flue gas purification system shown in Fig. 1 can realize the following integrated treatment to flue gas：First, flue gas is carried out
Dedusting；Then, desulphurization denitration is synchronized to the gas after dedusting；Hereafter, decarburization is carried out to the gas after desulphurization denitration；Decarburization
Tail gas afterwards is discharged.
Wherein, synchronized desulfuring and denitrifying includes following subprocess again：Sulfur dioxide and nitrogen oxides in I, gases are simultaneously
Absorbed by the first absorbing liquid containing oxidant and be oxidized to corresponding acid ion respectively so as in first absorbing liquid
The middle corresponding acid of generation (generally sulfuric acid and nitric acid)；Acid described in II, is respectively with entering the first alkalescence in the first absorbing liquid
Material reacts and generates the salt corresponding with the acid ion (being generally sulfate and nitrate) respectively；III, is reclaimed
Described salt.
Obviously, after the process and the decarburization that carry out decarburization in whole flue gas purification system operation to the gas after desulphurization denitration
Process is not necessarily carried out after said process II or process III.Term " need not " refer to can with but meaning not necessarily.
Below in conjunction with the composition of oxidant and the first alkaline matter in the first absorbing liquid 201, in the second absorbing liquid 301
The present embodiment is further detailed the composition of two alkaline matters.
According to the difference of the composition of the first alkaline matter in the first absorbing liquid 201, the present embodiment can be subdivided into four kinds of tools
The technique of body.For ease of description, these four specific techniques are now referred to as technique one, technique two, technique three and technique four.
The composition of oxidant and the first alkaline matter in the first absorbing liquid 201 that the technique one is related into technique four,
The composition and relevant chemical equation of second alkaline matter can be found in shown in table 1 in second absorbing liquid 301.
(videing infra)
Table 1
As shown in table 1, in the present embodiment, the first absorbing liquid is actually by water, oxidant and the first alkaline matter group
Into；Second absorbing liquid is made up of water, the second alkaline matter.As the use of the first absorbing liquid (the second absorbing liquid), first absorbs
The content of each component is dynamic change in liquid (the second absorbing liquid).But, those skilled in the art can be according to relevant bar
Part calculates the content of each component under the first absorbing liquid (the second absorbing liquid) original state.
When the first alkaline matter is carbonate, bicarbonate, the process II of synchronized desulfuring and denitrifying will produce carbon dioxide
Gas.For example, the process two in technique two in table 1 just there occurs following chemical reaction：
H2SO4+Ca(HCO3)2=CaSO4+2CO2↑+2H2O
2HNO3+Ca(HCO3)2=Ca (NO3)2+2CO2↑+2H2O
Because gas is gone to toward inherently containing carbon dioxide carrying out desulphurization denitration, meanwhile, when the first alkaline matter is
When carbonate, bicarbonate, carbon dioxide can be produced again in the process II of synchronized desulfuring and denitrifying, therefore, substantial amounts of carbon dioxide
Gas decarbonization system 300 will be entered so as to generate more carbonate and/or bicarbonate.And carbonate and bicarbonate are just
The first alkaline matter can be used as again.At this moment, so that it may which the carbonate and bicarbonate for generating gas decarbonization system 300 are used as
One alkaline matter and be back to the process II.
According to Fig. 1, in the spray absorber as gas decarbonization system 300 with being used as gas sweetening denitrating system
Carbonate, bicarbonate for will be generated in gas decarbonization system 300 are just connected between 200 spray absorber and is used as
One alkaline matter flows back in the conveyer 600 of gas sweetening denitrating system 200, to use carbonic acid when the first alkaline matter
When salt, bicarbonate can as used in gas decarbonization system 300 is supplied in gas sweetening denitrating system 200 first basic species
Matter.
It should also be noted that, also specially being enumerated in table 1 to the first alkaline matter, such as first in technique one
Alkaline matter can also use ammonium carbonate, ammonium hydrogen carbonate in addition to using ammonia.Those skilled in the art can be according to known chemical industry
Knowledge is found by the practice to the present invention, can be by being expected after desulphurization denitration using these first alkaline matters
Salt.
The signal of another gas sweetening denitrating systems of the Fig. 2 for the present invention and the flue gas purification system using the system
Figure.As shown in Fig. 2 the same gas dust remover 100 for including being sequentially connected of the flue gas purification system of the embodiment, gas sweetening take off
Nitre system 200, gas decarbonization system 300, blower fan 400 and tapping equipment 500；Distinguished with the flue gas purification system of previous embodiment
It is only that gas sweetening denitrating system 200 is different.
As shown in Fig. 2 gas sweetening denitrating system 200 includes first reactor 210 and second reactor 220, wherein, institute
Stating first reactor 210 uses the first absorbing liquid containing oxidant to absorb sulfur dioxide and nitrogen oxides in gas simultaneously simultaneously
They are oxidized to corresponding acid ion respectively to obtain corresponding acid in the recovered liquid that the first absorbing liquid changes
(generally sulfuric acid and nitric acid), the second reactor 220 is reacted and distinguished using the first alkaline matter and described acid
The generation salt corresponding with the acid ion (is generally sulfate and nitrate), the first reactor 210 and second anti-
The passage being connected between device 220 for transmitting the recovered liquid is answered, the second reactor 220 is connected with for anti-to second
Answer the alkali source feedway 221 that first alkaline matter is delivered in device 220.
It can be seen that, the gas sweetening method of denitration that the gas sweetening denitrating system 200 of latter embodiment is realized equally includes
Said process I and process II.Only, the gas sweetening denitrating system 200 of latter embodiment is to be arranged in the process I
Carried out in first reactor 210, the process II has been arranged in second reactor 220 and carried out, so, will be easy to according to need
To adjust the first alkaline matter to obtain different sulfate and nitrates by alkali source feedway 221.
Below in conjunction with the composition of oxidant, the first alkaline matter in the first absorbing liquid 201 composition to latter embodiment
It is further detailed.
Latter embodiment is equally subdivided into four kinds of specific techniques.For ease of description, now these four specific techniques are claimed
For technique five, technique six, technique seven and technique eight.
The composition of oxidant in the first absorbing liquid 201 that the technique five is related into technique eight, the first alkaline matter
Composition and relevant chemical equation can be found in shown in table 2.
Table 2
The part omitted in table 2 may be referred to corresponding content in table 1.In addition, being omitted in table 2 to decarbonizing process
Related description, equally refer to the related content in table 1.
It is pointed out that in the above embodiment of the present invention, sulfate that gas recovery system for desulfuration and denitration 200 is generated and
The technology of nitrate is existing, for example, can realize sulfate by concentration is carried out after the solution discharge of sulfate and nitrate
Reclaimed with nitrate.
Technique two is at will now extracted into technique eight from technique one, certain is handled with the corresponding flue gas purification system of technique two
Exemplified by the coal-fired flue-gas of power plant, illustrate the technique effect of the present invention.
Flue gas data of the coal-fired flue-gas after by gas dust remover are as shown in table 3.
Table 3
| Project | Unit | Data |
| SO2Content | mg/m3 | 128 |
| NOXContent | mg/m3 | 184 |
| Oxygen content | Volume % | 1.95 |
| Flue-gas temperature | ℃ | 110 |
| Dust content | mg/m3 | 23 |
| Flue gas flow | m3/h | 450000 |
Production time in year was computed based on 300 days, SO can be realized by the corresponding flue gas purification system of technique two2Emission reduction
415 tons/year, NOX596 tons/year of emission reduction；2344 tons/year of calcium nitrate, 882 tons/year of calcium sulfate, it is contemplated that income from sales is near can be produced
10000000 yuan.
Claims (10)
1. gas sweetening method of denitration, including procedure below：Sulfur dioxide and nitrogen oxides in I, gases are simultaneously by containing aerobic
First absorbing liquid of agent absorbs and is oxidized to corresponding acid ion respectively to generate phase in first absorbing liquid
The acid answered；Acid described in II, into the first alkaline matter in the first absorbing liquid respectively with reacting and generating respectively and institute
State the corresponding salt of acid ion；III, reclaims described salt.
2. the method as described in claim 1, it is characterised in that：The process I occurs in first reactor, and process II occurs
In second reactor；It is connected between the first reactor and second reactor and institute is passed through by the first absorbing liquid for transmitting
The passage of the recovered liquid changed after process I is stated, the second reactor is connected with for delivering institute into second reactor
State the alkali source feedway of the first alkaline matter.
3. the method as described in claim 1, it is characterised in that：The process I occurs in same reactor with process II；
Then, in the first absorbing liquid used in the process I not only containing the oxidant simultaneously again contain first alkaline matter.
4. the method as described in any one claim in claims 1 to 3, it is characterised in that：Titanium dioxide in the process I
Sulphur and nitrogen oxides are oxidized to sulfate ion and nitrate ion to generate sulfuric acid and nitre in the first absorbing liquid respectively
Acid；The sulfuric acid and nitric acid react and generation sulfate and nitric acid respectively with the first alkaline matter respectively in the process II
Salt.
5. the method as described in any one claim in claims 1 to 3, it is characterised in that：The oxidant is selected from double
The metal cation of the first alkaline matter in oxygen water and the process II is in the Peroxides and Superoxides of same metal
Any one or a few.
6. the method as described in any one claim in claims 1 to 3, it is characterised in that：First alkaline matter
Selected from ammonia, ammonium carbonate, ammonium hydrogen carbonate, calcium hydroxide, calcium oxide, calcium carbonate, calcium bicarbonate, potassium hydroxide, potassium carbonate, bicarbonate
Any one or a few in potassium, sodium hydroxide, sodium carbonate, sodium acid carbonate.
7. the method as described in any one claim in claims 1 to 3, it is characterised in that：Also including need not be described
The process IV carried out after process II or process III：The tail gas containing carbon dioxide that will do not absorbed by first absorbing liquid
Absorbed to be carbonate and/or bicarbonate by the carbon dioxide conversion with the second absorbing liquid containing the second alkaline matter
Salt.
8. method as claimed in claim 7, it is characterised in that：Second alkaline matter is selected from ammonia, calcium hydroxide, hydroxide
Any one or a few in potassium, sodium hydroxide.
9. method as claimed in claim 8, it is characterised in that：Second alkaline matter and the carbon dioxide reaction are given birth to
Into bicarbonate as the first alkaline matter be back to the process II.
10. the method as described in any one claim in claims 1 to 3, it is characterised in that：Including to institute will be entered
The gas for stating process I carries out the preprocessing process of dedusting.
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