CN107824039A - Composite oxidant and the method for dry desulfurization denitration - Google Patents
Composite oxidant and the method for dry desulfurization denitration Download PDFInfo
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- CN107824039A CN107824039A CN201711261628.7A CN201711261628A CN107824039A CN 107824039 A CN107824039 A CN 107824039A CN 201711261628 A CN201711261628 A CN 201711261628A CN 107824039 A CN107824039 A CN 107824039A
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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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- 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
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2251/00—Reactants
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- B01D2251/108—Halogens or halogen compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D2251/306—Alkali metal compounds of potassium
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Abstract
The invention discloses a kind of composite oxidant and the method for dry desulfurization denitration, the composite oxidant includes following component：The parts by weight of hypochlorite 10~20；The parts by weight of chlorite 40~60；The parts by weight of ferrate 1~20；The parts by weight of permanganate 1~20；The parts by weight of hydrogen peroxide 10~30；The parts by weight of thiosulfate 1~20；The parts by weight of citrate 1~5；With the parts by weight of aromatic carboxylic acid salt 1~5.The composite oxidant of the present invention can be combined with magnesia dry powder synchronizes desulphurization denitration to flue gas.
Description
Technical field
The present invention relates to a kind of composite oxidant and the method for dry desulfurization denitration, more particularly to a kind of flue gas desulfurization and denitrification
Composite oxidant and dry desulfurization denitration method.
Background technology
Contain sulfur dioxide and nitrogen oxides NO in flue gas simultaneouslyx, thus need to develop the technology of simultaneous SO_2 and NO removal, such as
Activated carbon method, SNOX techniques, SNRB techniques, NOXSO techniques and electronic beam method etc..These technologies are ripe not enough, can not be fine
Application.At present, most of power plant, Industrial Boiler still use single sulfur method and method of denitration.
The method species of independent denitration and independent desulfurization is various.SCR (SCR) technology is China power station pot
The major technique of stove denitration.SCR techniques can be divided into following several classes by the installation position according to SCR device：High grey segment process,
Low grey segment process and afterbody arrangement technology.The catalyst that high grey segment process uses is needed with stronger antiblocking ability, alkali resistant
Metal toxicity ability and anti-sulfur dioxide toxicity ability.The catalyst that low grey segment process uses is remained that with stronger anti-two
Sulfur oxide toxicity ability.Although the catalyst that afterbody arrangement technology uses needs from the murder by poisoning of high dust and sulfur dioxide
Want flue gas to reheat, thus waste mass energy.Therefore, there is still a need for exploitation low temperature SCR denitration system, adds so as to reduce flue gas
Hot link, and reduce energy consumption.
Sulfur method mainly has wet method, dry method and semidry method.Wet desulphurization is the most ripe sulfur method in coal-burning power plant, main
There are limestone/gypsum method, ammonia process, magnesium processes, Sea water respiratory distress syndrome etc..Wet desulphurization has that system complex, floor space be big, equipment
Seriously corroded, produce the problems such as a large amount of waste liquids.Dry desulfurization then have the characteristics that take up an area less, investment operating cost it is low, pollution-free,
Thus receive much concern.
The Chinese patent application of Application No. 201710515142.5 discloses a kind of loaded modified magnesia of monoethanolamine
Base flue gas dry desulfurizing adsorbent and preparation method, using magnesia as raw material, magnesium oxide-based adsorbent is prepared using coprecipitation,
Roasting initial stage, by pyrolysis, the volatile impurities such as chemical bonding water and carbon therein can be removed, change into absorption and lived
The magnesia of property, by the recrystallization of catabolite, also obtains having the magnesium oxide-based of specific crystal formation, grain size and pore structure
Adsorbent, the specific surface area of magnesium oxide-based adsorbent is increased, and at relatively high temperatures, solid phase reaction, shape also occur for magnesia
Into active combined form, the performance of desulfurization is also improved therewith, and monoethanolamine finally is carried on into adsorbent with infusion process again
Surface, for chemisorbed desulfurization, obtained desulfuration adsorbent intensity is high, carries out flue gas dry desulfurizing.This method is needed to oxygen
Change magnesium and carry out specially treated, because flue gas desulfurization needs to use substantial amounts of desulfurizing agent, cause flue gas desulfurization cost to improve, and its
Flue gas desulfurization is can be only used for, and denitrating flue gas can not be carried out.
The Chinese patent application of Application No. 200610017524.7 discloses a kind of circulation dry-phase flow tower flue gas dry method
Sulfur removal technology：(1) form waste gas of sulfur dioxide will be contained caused by industrial production first to be sent into primary dust removing device, removed in flue gas
90% fly ash particulate；(2) flue gas for removing fly ash particulate is sent into circulation dry-phase flow tower and in flue gas by pipeline
The equally distributed desulfurization absorbent slurries magnesia in porch fully contacts, and makes by the power of flue gas in absorbent slurry and flue gas
Sulfur dioxide be mixed into tower, multigroup agitator is set in tower, mixture is thoroughly mixed reaction, generation sulfurous acid
Magnesium and magnesium sulfate, reach desulfurization purpose；(3) flue gas reacted is sent to two level by circulation dry-phase flow tower gas-solid separator and removed
Dirt device, the qualified discharge after dedusting again, while in tower reactant in the presence of bottom of towe particle sorter, by accessory substance and
The desulfurization absorbent particulate matter not reacted completely sorts away, the desulfurization absorbent particle not reacted completely that will be can be recycled
Thing sends recycle unit, repeated recycling utilize back to by circulation dry-phase flow tower bottom of towe chain conveyor.The technique is not used to cigarette
Qi exhaustion nitre.In addition, the technique mixes magnesia with flue gas in smoke inlet in form of slurry, subsequently into desulfurizing tower, lead
The two is caused not react fully so that desulfuration efficiency is only capable of reaching 90%.
To sum up, still flue gas desulfurization is carried out without a kind of directly combined using alkaline absorbent dry powder with composite oxidant at present
The report of denitration.
The content of the invention
It is an object of the present invention to provide a kind of composite oxidant, and it is used in combination with alkaline absorbent dry powder,
Flue gas synchronized desulfuring and denitrifying can be carried out.According to further aim of the present invention, the composite oxidant can be at a lower temperature
Carry out flue gas desulfurization and denitrification.
It is another object of the present invention to provide a kind of method of flue gas dry desulfurizing denitration, and it is directly inhaled using alkalescence
Agent dry method synchronized desulfuring and denitrifying is received, and denitrification efficiency is high.
According to an aspect of the present invention, the present invention provides a kind of composite oxidant, including following component：
According to the composite oxidant of the present invention, it is preferable that the hypochlorite is selected from the hypochlorite of alkali metal；The Asia
Chlorate is selected from the chlorite of alkali metal；The ferrate is selected from the ferrate of alkali metal；The permanganate is selected from
The permanganate of alkali metal；The thiosulfate is selected from the thiosulfate of alkali metal；The citrate is selected from alkali metal
Citrate；The aromatic carboxylic acid salt is selected from the aromatic carboxylic acid salt of alkali metal.
According to the composite oxidant of the present invention, it is preferable that the hypochlorite of the alkali metal is sodium hypochlorite or hypochlorous acid
Potassium；The chlorite of the alkali metal is sodium chlorite or potassium chlorite；The ferrate of the alkali metal is potassium ferrate；Institute
The permanganate for stating alkali metal is potassium permanganate；The thiosulfate of the alkali metal is sodium thiosulfate or potassium thiosulfate；
The citrate of the alkali metal is sodium citrate；The aromatic carboxylic acid salt of the alkali metal is aromatic carboxylic acid sodium.
According to the composite oxidant of the present invention, it is preferable that one kind in following material of the aromatic carboxylic acid salt or
It is a variety of：
In formula (I), (II) and (III), n is 0~6 natural number, and R is alkali metal ion.
According to the composite oxidant of the present invention, it is preferable that the composite oxidant is for flue gas dry desulfurizing denitration
Oxidant.
According to another aspect of the present invention, the present invention provides a kind of method of dry desulfurization denitration, is absorbed using alkalescence
Agent dry powder and above-mentioned composite oxidant, which combine, carries out flue gas dry desulfurizing denitration.
Method in accordance with the invention it is preferred that comprise the following steps：
(1) former flue gas is subjected to pre- dust removal process, obtains the flue gas after dedusting；The dustiness in flue gas after the dedusting
For 10~30mg/Nm3；
(2) alkaline absorbent dry powder is well mixed with the flue gas after the dedusting in flue, subsequently into following
Ring fluid bed absorption tower, the aqueous solution containing composite oxidant is sprayed into the recirculating fluidized bed absorption tower, the cigarette after the dedusting
Gas is converted into desulphurization denitration flue gas；Wherein, the flue is arranged on the outside on the recirculating fluidized bed absorption tower.
Method in accordance with the invention it is preferred that in step (1), the temperature of former flue gas is 80~150 DEG C, flow velocity is 2~
5m/s, sulfur dioxide concentration are 1000~3000mg/Nm3, and nitrous oxides concentration is 200~500mg/Nm3。
Method in accordance with the invention it is preferred that in step (2), the alkaline absorbent dry powder and the cigarette after the dedusting
Time of contact of the gas in the recirculating fluidized bed absorption tower is in more than 30min.
Method in accordance with the invention it is preferred that methods described also comprises the following steps：
(3) the desulphurization denitration flue gas is subjected to dust removal process, is purified flue gas, accessory substance and the alkali not reacted completely
Property absorbent dry powder, and the alkaline absorbent dry powder not reacted completely is sent into institute from the bottom on the recirculating fluidized bed absorption tower
State recirculating fluidized bed absorption tower.
Combined using the composite oxidant of the present invention with alkaline absorbent dry powder, flue gas can be carried out at a lower temperature
Synchronized desulfuring and denitrifying.Oxidizing lower nitrogen oxides (such as NO) is forced using composite oxidant, it is converted into and is more readily absorbed
Higher nitrogen oxides (such as NO of removal2), so that alkaline absorbent dry powder denitration is possibly realized.The method of the present invention is direct
Fully contacted with flue gas using alkaline absorbent dry powder, can more efficiently remove the sulfur dioxide and nitrogen oxides in flue gas.
According to currently preferred technical scheme, the desulfuration efficiency of this method is more than 93%, and denitration efficiency is more than 85%.
Embodiment
With reference to specific embodiment, the present invention is further illustrated, but protection scope of the present invention is not limited to
This.
<Composite oxidant>
The composite oxidant of the present invention includes strong oxidizer and buffer etc..By these component rational proportions, can improve
It is to sulfur dioxide and the oxidation effectiveness of lower nitrogen oxides (such as NO).The composite oxidant of the present invention can include such as the following group
Point：
According to an embodiment of the invention, the composite oxidant includes following component：
Said components are made into the aqueous solution by the present invention, are directly used in flue gas desulfurization and denitrification, it is not necessary to flue gas is heated,
Also without progress ultraviolet radiation activated, thus energy resource consumption can be reduced.In the present invention, hypochlorite, chlorite
In Cl be in+1 valency ,+trivalent, the Fe in ferrate is in+6 valencys, and the Mn in permanganate is in+7 valencys, the O in hydrogen peroxide
S in -1 valency, thiosulfate is in+7 valencys.These elements are in high-valence state, have stronger oxidisability.These groups
It can be sulfur trioxide by the oxidizing sulfur dioxide in flue gas to divide, and lower nitrogen oxides (such as NO) are oxidized into high price nitrogen oxidation
Thing (such as NO2).It is a discovery of the invention that these components are used cooperatively, it can more efficiently promote above-mentioned oxidation reaction relatively low
At a temperature of carry out, so as to improve flue gas desulfurization and denitrification effect.
In the present invention, hypochlorite, chlorite, ferrate, permanganate, thiosulfate, citrate, fragrance
Race's carboxylate can be water soluble salt, such as alkali metal salt.So it is more beneficial for preparing solution and participates in desulfurization and denitrification reaction.
The example of alkali metal includes but is not limited to lithium, sodium, potassium etc..
In the present invention, hypochlorite can be water soluble hypochlorite, such as the hypochlorite of alkali metal；It is specific real
Example includes but is not limited to sodium hypochlorite or postassium hypochlorite.Chlorite can be Water soluble chlorite salts, such as the Asia of alkali metal
Chlorate；Specific example includes but is not limited to sodium chlorite or potassium chlorite.Ferrate can be water-soluble ferrate,
Such as the ferrate of alkali metal；Specific example includes but is not limited to potassium ferrate.Permanganate can be water-soluble Gao Meng
Hydrochlorate, such as the permanganate of alkali metal；Specific example includes but is not limited to potassium permanganate.Thiosulfate can be water-soluble
Property thiosulfate, such as the thiosulfate of alkali metal；Specific example includes but is not limited to sodium thiosulfate or thio sulphur
Sour potassium.Citrate can be water-soluble citrate, the citrate of alkali metal；Specific example includes but is not limited to lemon
Sour sodium.Aromatic carboxylic acid salt can be water-soluble aromatic race carboxylate, such as the aromatic carboxylic acid salt of alkali metal；Specific example
Including but not limited to aromatic carboxylic acid sodium.
In the present invention, aromatic carboxylic acid salt represent with aromatic rings carboxylate, these aromatic rings can be phenyl ring and
Its derivative, naphthalene nucleus and its derivative etc..According to an embodiment of the invention, aromatic carboxylic acid salt is in following material
One or more：
In formula (I), (II) and (III), n is 0~6 natural number, and R is alkali metal ion.The example bag of alkali metal ion
Include but be not limited to lithium ion, sodium ion, potassium ion etc..N is preferably 0~3.The example of aromatic carboxylic acid salt includes but is not limited to benzene
Sodium formate, sodium phenylacetate, benzenpropanoic acid sodium, para-phthalic sodium, to phenylenediacetic Acid sodium, to benzene dipropionic acid, M-phthalic acid sodium,
Isophthalic sodium diacelate, isophthalic dipropionic acid.It is a discovery of the invention that above-mentioned carboxylate is very beneficial for improving dry desulfurization denitration effect
Fruit.
In the present invention, the composite oxidant is the oxidant for flue gas dry desulfurizing denitration.Itself and alkalescence are inhaled
Receive agent dry powder to combine, can directly carry out dry desulfurization denitration.
The present invention can also relate to application of the above-mentioned composite oxidant in flue gas dry desulfurizing denitration, will contain composite oxygen
The aqueous solution atomization of agent is less than 5 μm of drop for diameter, the absorption tower containing flue gas is then sprayed into, so as to carry out flue gas desulfurization
Denitration.The less drop of size has good gas phase property and reactivity in flue gas.Sulfur dioxide in flue gas and low
Valency nitrogen oxides and the drop contact, are sulfur trioxide and higher nitrogen oxides by Quick Oxidation.Containing composite oxidant
In the aqueous solution, the concentration of composite oxidant is 500~3000mg/L.
<The method of dry desulfurization denitration>
The dry desulfurization method of denitration of the present invention is flue gas processing method, and it can carry out the comprehensive regulation to flue gas simultaneously,
So as to remove the sulfur dioxide and nitrogen oxides in flue gas simultaneously.In the method for the invention, using alkaline absorbent dry powder and
Above-mentioned composite oxidant, which combines, carries out flue gas dry desulfurizing denitration.Composite oxidant can be used in a manner of the aqueous solution.At this
In the aqueous solution, the concentration of composite oxidant is 500~3000mg/L.Preferably, the aqueous solution be atomized for diameter be less than 5 μm,
Preferably smaller than 3 μm of drop.
The method of the present invention can include pre- dust removal step, desulphurization denitration step；Optionally, dedusting can also be included and followed
Ring step etc..Introduce in detail below.
Pre- dust removal step：
The pre- dust removal step of the present invention is that former flue gas is carried out into pre- dust removal process, obtains the flue gas after dedusting；The dedusting
The dustiness in flue gas afterwards is 10~30mg/Nm3.Pre- dust removal process can use cloth-sack-type dust removal, spiral-flow type dedusting or
The method of electric precipitation, and preferably electric precipitation.By pre- dust removal step, particle larger and small in flue gas can be removed.Remove
Dustiness is 10~30mg/Nm in flue gas after dirt3, preferably 10~20mg/Nm3, more preferably 10~15mg/Nm3.When except
When the dustiness in flue gas after dirt is above range, composite oxidant and the lower nitrogen oxides in flue gas, dioxy can be made
Change sulphur more fully to react, so as to form sulfur trioxide and NO2、N2O5Etc. high-valence state nitrogen oxides.
In the present invention, the temperature of the former flue gas before pre- dust removal process can be 80~150 DEG C, preferably 110~130
℃.The flow velocity of former flue gas is 2~5m/s, preferably 2~4m/s, more preferably 2~3.5m/s.By flue-gas temperature and flow control
In above range, advantageously the lower nitrogen oxides in composite oxidant and flue gas, sulfur dioxide reaction, de- so as to improve
Sulphur denitration efficiency.
In the present invention, the sulfur dioxide SO of former flue gas2Concentration is 1000~3000mg/Nm3, more preferably 1500~
2500mg/Nm3.The nitrogen oxides NO of former flue gasxConcentration is 200~500mg/Nm3, more preferably 300~450mg/Nm3.By cigarette
Sulfur dioxide and the nitrous oxides concentration control of gas are in above range, the advantageously Low-Charged Nitrogen in composite oxidant and flue gas
Oxide, sulfur dioxide reaction, so as to improve denitrification efficiency.
Desulphurization denitration step：
The desulphurization denitration step of the present invention be by the flue gas after alkaline absorbent dry powder and the dedusting in flue
It is well mixed, subsequently into recirculating fluidized bed absorption tower, the aqueous solution containing composite oxidant is sprayed into the recirculating fluidized bed and inhaled
Tower is received, the flue gas after the dedusting is converted into desulphurization denitration flue gas.Flue is arranged on the recirculating fluidized bed absorption tower
It is outside.The present invention is well mixed using alkaline absorbent dry powder with flue gas in flue, subsequently into absorption tower.So may be used
Effectively to avoid because the presence of water causes alkaline absorbent dry powder to be reunited, so that alkaline absorbent dry powder can not with flue gas
It is well mixed.Such setting can improve flue gas desulfurization and denitrification effect.
In the present invention, the aqueous solution atomization containing composite oxidant is less than to 5 μm of drop for diameter, is then sprayed into and follows
Ring fluid bed absorption tower.It is for instance possible to use the aqueous solution containing composite oxidant is atomized by sprayer.The less drop of size
There is good gas phase property and reactivity in flue gas.Sulfur dioxide and lower nitrogen oxides in flue gas connect with the drop
Touch, be sulfur trioxide and higher nitrogen oxides by Quick Oxidation.In the aqueous solution containing composite oxidant, composite oxidant it is dense
Spend for 500~3000mg/L, such as 600~1500mg/L.The entrance of sprayer is arranged on the text on recirculating fluidized bed absorption tower
The top of venturi, the quantity of entrance are 3~5, with ensure flue gas in the aqueous solution and tower containing composite oxidant and
Alkaline absorbent fully contacts.
In the present invention, the flue gas after alkaline absorbent dry powder and the dedusting is in the recirculating fluidized bed absorption tower
Time of contact can be more than 30min, such as 30~60min.Alkaline absorbent dry powder repeatedly circulates in absorption tower, makes itself and cigarette
The time of contact increase of gas is general up to more than 30min.Sulfur trioxide and high-valence state nitrogen oxides react with alkaline absorbent,
Sulfate and nitrate is generated, so as to reach the effect of desulphurization denitration.In the present invention, alkaline absorbent is selected from calcium oxide, oxygen
Change the alkaline matter such as magnesium or sodium hydroxide.According to an embodiment of the invention, the content of magnesia of alkaline absorbent exists
More than 80wt%.According to a preferred embodiment of the present invention, alkaline absorbent is magnesia dry powder.For example with active oxygen
Change the magnesia dry powder that content of magnesium is 80~85wt%.It is a discovery of the invention that alkaline absorbent and composite oxidant as using
Synergy, can more efficiently promote flue gas desulfurization and denitrification.
Dedusting and circulation step：
The dust removal step of the present invention is that the desulphurization denitration flue gas is carried out into dust removal process, is purified flue gas, accessory substance
The magnesia dry powder not reacted completely, and by the magnesia dry powder not reacted completely from the bottom on the recirculating fluidized bed absorption tower
Portion is sent into the recirculating fluidized bed absorption tower.According to an embodiment of the invention, the dust removal process is in sack cleaner
Middle progress.Under gravity, the complete alkalescence of sulfate, nitrate and unreacted flue gas desulfurization and denitrification formed absorbs
Agent separates.Sulfate, nitrate enter accessory substance storehouse as accessory substance；The complete alkaline absorbent of unreacted reenters absorption
Reused in tower；Purifying smoke is through smoke stack emission.
Embodiment 1
(1) former flue gas (oxygen content 15vol%, flow velocity 3.5m/s) is removed into particulate matter using electric precipitation, obtained
It is 15mg/Nm to dustiness3Dedusting after flue gas.Former flue gas (inlet flue gas) parameter is as shown in table 1.
(2) by the flue gas after magnesia dry powder and dedusting in the flue being arranged on outside recirculating fluidized bed absorption tower
It is well mixed, subsequently into recirculating fluidized bed absorption tower, the aqueous solution containing composite oxidant is sprayed into this by sprayer and followed
Ring fluid bed absorption tower, liquid-drop diameter are less than 5 microns.The formula of composite oxidant is referring to table 2.Composite oxidant in the aqueous solution
Concentration is 1000mg/L.The entrance of sprayer is arranged on the top of the Venturi tube on recirculating fluidized bed absorption tower, entrance
Quantity is 5, to ensure that the aqueous solution containing composite oxidant fully contacts with the flue gas in tower and magnesia.Magnesia is done
Flue gas after powder, the aqueous solution containing composite oxidant and dedusting fully contacts 30min.In recirculating fluidized bed absorption tower, spray
The atomization composite oxidant drop entered contacts with the sulfur dioxide in flue gas and lower nitrogen oxides (such as NO), in vapor-liquid two phases
Interface, redox reaction quickly occurs, sulfur dioxide and lower nitrogen oxides (such as NO) are oxidized to sulfur trioxide and high price
Nitrogen oxides (such as NO2)；The latter is oxidized magnesium and absorbs generation sulfate and nitrate, is taken off so as to synchronously complete the desulfurization of flue gas
Nitre, form desulphurization denitration flue gas.
(3) desulphurization denitration flue gas is subjected to dust removal process using sack cleaner, is purified flue gas, accessory substance and not complete
The magnesia dry powder of full response.Accessory substance is mainly magnesium sulfate and magnesium nitrate.By the magnesia dry powder not reacted completely from circulation
Recirculating fluidized bed absorption tower, recycling are sent into the bottom on fluid bed absorption tower.The parameter of purifying smoke is as shown in table 3.
Table 1, inlet flue gas parameter
| Sequence number | Parameter | Unit | Numerical value |
| 1 | Exhaust gas volumn (operating mode) | m3/h | 180000 |
| 2 | Standard state exhaust gas volumn | Nm3/h | 120441 |
| 2 | Entrance sulfur dioxide concentration | mg/Nm3 | 2200 |
| 3 | Entrance nitric oxide concentration | mg/Nm3 | 350 |
| 4 | Inlet dust | mg/Nm3 | 115 |
| 5 | Flue-gas temperature | ℃ | 120 |
| 6 | Humidity of flue gas | % | 6.7 |
Table 2, combined oxidation agent prescription
| Sodium hypochlorite | 20 parts by weight |
| Sodium chlorite | 45 parts by weight |
| Potassium ferrate | 5 parts by weight |
| Potassium permanganate | 5 mass point |
| Hydrogen peroxide | 15 parts by weight |
| Sodium thiosulfate | 5 parts by weight |
| Sodium citrate | 2 parts by weight |
| Sodium benzoate | 3 parts by weight |
Table 3, exiting flue gas parameter
| Sequence number | Project | Quantity | Unit |
| 1 | Exiting flue gas amount (operating mode) | 436765 | m3/h |
| 2 | Exhaust gas temperature | 65 | ℃ |
| 3 | Sulfur dioxide emissioning concentration | 36 | mg/Nm3 |
| 4 | Desulfuration efficiency | 98.36 | % |
| 5 | Discharged nitrous oxides concentration | 48 | mg/Nm3 |
| 6 | Denitration efficiency | 86.29 | % |
| 7 | The quantum of output of accessory substance | 5.71 | t/h |
Embodiment 2
Except the formula shown in the formula substitution table 2 using table 4, remaining condition is same as Example 1, gained purifying smoke
Parameter is referring to table 5.
Table 4, combined oxidation agent prescription
| Sodium hypochlorite | 10 parts by weight |
| Sodium chlorite | 50 parts by weight |
| Potassium ferrate | 5 parts by weight |
| Potassium permanganate | 5 mass point |
| Hydrogen peroxide | 20 parts by weight |
| Sodium thiosulfate | 5 parts by weight |
| Sodium citrate | 2 parts by weight |
| Sodium benzoate | 3 parts by weight |
Table 5, exiting flue gas parameter
| Sequence number | Project | Quantity | Unit |
| 1 | Exiting flue gas amount (operating mode) | 424567 | m3/h |
| 2 | Exhaust gas temperature | 65 | ℃ |
| 3 | Sulfur dioxide emissioning concentration | 35 | mg/Nm3 |
| 4 | Desulfuration efficiency | 98.40 | % |
| 5 | Discharged nitrous oxides concentration | 39 | mg/Nm3 |
| 6 | Denitration efficiency | 88.86 | % |
| 7 | The quantum of output of accessory substance | 5.57 | t/h |
Embodiment 3
Except the formula shown in the formula substitution table 2 using table 6, remaining condition is same as Example 1, gained purifying smoke
Parameter is referring to table 7.
Table 6, combined oxidation agent prescription
| Sodium hypochlorite | 10 parts by weight |
| Sodium chlorite | 55 parts by weight |
| Potassium ferrate | 5 parts by weight |
| Potassium permanganate | 5 mass point |
| Hydrogen peroxide | 10 parts by weight |
| Sodium thiosulfate | 5 parts by weight |
| Sodium citrate | 2 parts by weight |
| Para-phthalic sodium | 3 parts by weight |
Table 7, exiting flue gas parameter
| Sequence number | Project | Quantity | Unit |
| 1 | Desulfurizing tower exiting flue gas amount (operating mode) | 413643 | m3/h |
| 2 | Exhaust gas temperature | 65 | ℃ |
| 3 | Sulfur dioxide emissioning concentration | 17 | mg/Nm3 |
| 4 | Desulfuration efficiency | 99.23 | % |
| 5 | Discharged nitrous oxides concentration | 30 | mg/Nm3 |
| 6 | Denitration efficiency | 91.43 | % |
| 7 | The quantum of output of accessory substance | 5.61 | t/h |
The present invention is not limited to above-mentioned embodiment, in the case of without departing substantially from the substantive content of the present invention, this area skill
Any deformation, improvement, the replacement that art personnel are contemplated that each fall within the scope of the present invention.
Claims (10)
1. a kind of composite oxidant, it is characterised in that including following component：
2. composite oxidant according to claim 1, it is characterised in that the hypochlorite is selected from the hypochlorous acid of alkali metal
Salt；The chlorite is selected from the chlorite of alkali metal；The ferrate is selected from the ferrate of alkali metal；The Gao Meng
Hydrochlorate is selected from the permanganate of alkali metal；The thiosulfate is selected from the thiosulfate of alkali metal；The citrate choosing
From the citrate of alkali metal；The aromatic carboxylic acid salt is selected from the aromatic carboxylic acid salt of alkali metal.
3. composite oxidant according to claim 2, it is characterised in that the hypochlorite of the alkali metal is sodium hypochlorite
Or postassium hypochlorite；The chlorite of the alkali metal is sodium chlorite or potassium chlorite；The ferrate of the alkali metal is height
Potassium ferrite；The permanganate of the alkali metal is potassium permanganate；The thiosulfate of the alkali metal is sodium thiosulfate or sulphur
Potassium thiosulfate；The citrate of the alkali metal is sodium citrate；The aromatic carboxylic acid salt of the alkali metal is aromatic carboxylic acid
Sodium.
4. composite oxidant according to claim 2, it is characterised in that the aromatic carboxylic acid salt is in following material
One or more：
In formula (I), (II) and (III), n is 0~6 natural number, and R is alkali metal ion.
5. according to the composite oxidant described in any one of Claims 1 to 4, it is characterised in that the composite oxidant be for
The oxidant of flue gas dry desulfurizing denitration.
A kind of 6. method of dry desulfurization denitration, it is characterised in that using alkaline absorbent dry powder and as Claims 1 to 5 is appointed
Composite oxidant described in one, which combines, carries out flue gas dry desulfurizing denitration.
7. according to the method for claim 6, it is characterised in that comprise the following steps：
(1) former flue gas is subjected to pre- dust removal process, obtains the flue gas after dedusting；The dustiness in flue gas after the dedusting is 10
~30mg/Nm3；
(2) alkaline absorbent dry powder is well mixed with the flue gas after the dedusting in flue, subsequently into recycle stream
Change bed absorption tower, the aqueous solution containing composite oxidant is sprayed into the recirculating fluidized bed absorption tower, the flue gas after the dedusting turns
Turn to desulphurization denitration flue gas；Wherein, the flue is arranged on the outside on the recirculating fluidized bed absorption tower.
8. according to the method for claim 7, it is characterised in that in step (1), the temperature of former flue gas is 80~150 DEG C, stream
Speed is 2~5m/s, and sulfur dioxide concentration is 1000~3000mg/Nm3, and nitrous oxides concentration is 200~500mg/Nm3。
9. according to the method for claim 7, it is characterised in that in step (2), the alkaline absorbent dry powder removes with described
Time of contact of the flue gas in the recirculating fluidized bed absorption tower after dirt is in more than 30min.
10. according to the method described in any one of claim 6~9, it is characterised in that methods described also comprises the following steps：
(3) the desulphurization denitration flue gas is subjected to dust removal process, is purified flue gas, accessory substance and the alkalescence suction do not reacted completely
Agent dry powder is received, and will be followed described in the alkaline absorbent dry powder not reacted completely from the bottom on recirculating fluidized bed absorption tower feeding
Ring fluid bed absorption tower.
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| CN109276987A (en) * | 2018-10-25 | 2019-01-29 | 中国石油化工股份有限公司 | A kind of absorbent for the processing of industrial tail gas desulphurization denitration |
| WO2021134925A1 (en) * | 2019-12-30 | 2021-07-08 | 童裳慧 | Semi-dry flue gas desulfurization and denitrification method |
| CN113457421A (en) * | 2021-07-24 | 2021-10-01 | 德清绿能热电有限公司 | Oxidation absorption liquid for boiler flue gas treatment and boiler flue gas treatment system |
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