CN109731450A - A two-stage flue gas post-treatment process - Google Patents
A two-stage flue gas post-treatment process Download PDFInfo
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Abstract
本发明涉及一种两段式烟气后处理工艺，该工艺包括协同式脱硫脱硝工艺段和碳酸氢钠再生工艺段，其中利用碳酸氢钠吸收烟气中二氧化硫的反应过程中生成的Na2SO3协同吸收氧化后的氮氧化物从而实现了协同式脱硫脱硝，进一步在上述脱除工艺后，利用加入碳酸氢钙的方式对反应副产物进行了再生利用，使得能够实现再生过程中各中间物质之间的简单有效分离。
The invention relates to a two-stage flue gas post-treatment process, which comprises a synergistic desulfurization and denitration process section and a sodium bicarbonate regeneration process section, wherein Na2SO3 generated in the reaction process of absorbing sulfur dioxide in flue gas by using sodium bicarbonate is cooperatively absorbed The oxidized nitrogen oxides thus realize synergistic desulfurization and denitrification. After the above-mentioned removal process, the by-products of the reaction are regenerated by adding calcium bicarbonate, so that the intermediary substances in the regeneration process can be realized. Simple and effective separation.
Description
Technical field
The present invention relates to after environmental protection technical field more particularly to a kind of two-part flue gas for gas cleaning
Science and engineering skill.
Background technique
Although China environmental protection obtains positive progress, but basic solution is not yet received in the overall deteriorating trend of environmental aspect
Certainly, atmosphere pollution is polluted from coal smoke type to region composite type and is changed.Regional Brownish haze phenomenon takes place frequently, and compound atmosphere is dirty
Dye becomes increasingly conspicuous, and it is practical that existing contamination control dynamics, which is difficult to meet an urgent demand of the people to air quality is improved,
Improve atmosphere quality, it is necessary to take stringenter measure, on the basis of digesting huge new increment, significantly cut down
Gross contamination emission.After after early stage, nitrogen oxides (NOx) is classified as restrictive Con trolling index by related environmental protection planning, current phase
The clear discharge that sulfur dioxide (SO2), NOx are further controlled from total amount in planning is protected in cyclization.
During long-term research, development and application, up to more than 250 kinds of flue gas desulfurization process, and obtain industry
Only more than ten of application value.Flue gas desulfurization technique is divided into wet process, semidry method and dry method according to operating method.China's desulfurization
The technology early stage of development mostly uses wet process technology, wherein being accounted for the largest percentage especially with wet-type calcium desulfuration technology.Wet desulphurization
Technique can guarantee 98% or more desulfuration efficiency, while there is also the processing of the secondary pollution of waste water, desulfurization product is number
The problems such as tired, smog discharge temperature is unfavorable for discharge diffusion lower than 60 DEG C, complex process and investment are larger.
In recent years, country advocates use semidry method, dry process desulfurization and dedusting energetically.Relative to wet desulphurization work
For skill, semidry method and dry process are simple, and dry state product is easily handled, and no waste water generates, no equipment corrosion, and investment is general
Lower than conventional wet.In addition, improved day by day with dry desulfurizing process, the continuous improvement of Pollutant-degrading gene is added
Its some advantage relative to conventional wet, so that the trend of current flue gas desulfurization technique development is gradually taken off from wet process to dry method
Sulphur dust collecting process technical change.
Flue gas is discharged for sintering, coking and Industrial Stoves etc., is mainly characterized by that exhaust gas temperature is low, smoke components
Complexity, traditional SCR denitration technology are difficult to apply, it is necessary to find new processing method.Also, the pollutant of flue gas is controlled
The development trend of reason technology is to be changed in terms of multi-pollutant Collaborative Control from the control of Single Pollution object.
It has been proposed that carrying out dry desulfurization using sodium bicarbonate, but found in practice, using only sodium bicarbonate to flue gas
The removal efficiency that middle sulfur dioxide is removed is not high, while cannot achieve the removing of nitrogen oxides in effluent, therefore often need
Denitrification apparatus is individually added, the situation that fixed investment is at high cost, removal effect is undesirable is caused.
Meanwhile in order to further decrease the longtime running cost of flue gas purification device, people it is expected always to gas cleaning
By-product carries out recycling processing after reaction.In this respect, it is thus proposed that after reacting all of ammonium hydrogen carbonate gas cleaning
By-product regenerated.In practice, it has been found that sodium bicarbonate and ammonium sulfate solubility curve due to being generated in regenerative process
Difference is small, and using its regeneration, there are two kinds of substance crystallizations in regenerative process to separate difficulty, and tight for the control condition of crystallization
Lattice are applied to and invest problem at high cost and that operation is complicated in engineering.Although the above method can be completed de- to sodium bicarbonate
The regeneration of product, but complex process are generated during sulphur, it is at high cost, it is difficult to apply in engineering production process.
Therefore, it is necessary to a kind of two-part flue gas aftertreatment technology for gas cleaning be proposed, to solve above-mentioned existing
There is the deficiency in technology.
Summary of the invention
A series of concept of reduced forms is introduced in Summary, this will in the detailed description section
It is further described.Summary of the invention is not meant to attempt to limit technical side claimed
The key feature and essential features of case, do not mean that the protection scope for attempting to determine technical solution claimed more.
In order to solve at least one of above-mentioned many deficiencies in the prior art, the invention discloses a kind of two-parts
Flue gas aftertreatment technology, wherein the technique includes cooperating type desulfurizing and denitrifying process section and sodium bicarbonate regeneration technology section, wherein
The cooperating type desulfurizing and denitrifying process section is the following steps are included: step A: spraying into oxidant with atomizing type into flue to realize
Gaseous oxidation to nitric oxide contained in flue gas in flue (NO) is nitrogen oxides；Step B: into flue with fine powder side
Formula sprays into sodium bicarbonate particle object to realize to sulfur dioxide contained in flue gas in flue (SO2) and the nitrogen oxides generated
Joint absorb and obtain the byproduct of reaction comprising including sodium sulphate, sodium nitrate and sodium carbonate；Step C: above-mentioned reaction will be contained
The flue gas of product carries out trapping processing by deduster, and treated, and flue gas is discharged into atmosphere, and the byproduct of reaction of trapping is via defeated ash
System is collected in by-product storehouse；The sodium bicarbonate is carried out again after flue gas removes after cooperating type desulfurizing and denitrifying process section
Raw process section, wherein the sodium bicarbonate regeneration technology section includes: step D: the by-product collected in by-product storehouse is discharged into dissolution
Solution is made in tank, and is added into solution to consume the dilute sulfuric acid of the sodium carbonate in by-product to obtain sodium sulphate and nitre
The level-one mixed liquor of sour sodium；Step E: above-mentioned level-one mixed liquor is sent into reactor and is reacted with calcium bicarbonate to be made
The second level mixed liquor of sodium bicarbonate, calcium sulfate and sodium nitrate；Step F: crystallization treatment is carried out to generate two to second level mixed liquor
Hydrated calcium sulfate, and the gypsum isolated after eddy flow is dehydrated and the three-level mixed liquor by sodium bicarbonate and sodium nitrate；Step
Rapid G: ammonium hydrogen carbonate is added into three-level mixed liquor and is reacted so that the level Four mixed liquor of sodium bicarbonate and ammonium nitrate is made；Step
Rapid H；Crystallization treatment is carried out to separate obtained sodium bicarbonate powder and ammonium nitrate to level Four mixed liquor.
Two-part flue gas aftertreatment technology according to the present invention, compared with prior art, the present invention utilize sodium bicarbonate
The mechanism that powder absorbs the NO after the Na2SO3 collaboration absorption oxidation generated in SO2 reaction process in flue gas is realized while being taken off
Sulphur denitration, and due to the absorption of mutually promoting in SO2 and NOx collaboration absorption process, desulfuration efficiency of the invention wants high
Desulfuration efficiency when desulfurization single using sodium bicarbonate powder in the prior art.
Further, the product generated after technique desulphurization denitration of the invention is used as Na2SO4, NaNO3, NaNO2 and is lacked
The mixture of Na2CO3 is measured, the present invention is reacted to obtain gypsum and sodium bicarbonate and nitre using Ca (HCO3) 2 and NH4HCO3
Sour ammonium.Conventional by-product sodium bicarbonate and sulfuric acid small different from solubility curve difference in the prior art, separation is difficult
Ammonium, it is sodium bicarbonate and ammonium nitrate that the need in the present invention, which carry out the by-product of Crystallization Separation, and the two solubility curve difference is obvious
Increase, makes it possible to simply separate two kinds of substance crystallizations, to reduce construction investment cost.
Preferably, the oxidant in step is the hydrogen peroxide of ozone or 10%, wherein by the oxidant
Dosage is set as making nitrogen dioxide and nitric oxide production molar ratio in flue gas to be greater than 1.
Preferably, the partial size of the sodium bicarbonate particle object sprayed into stepb into flue is at 20 μm hereinafter, and through gas
Power conveying, which sprays into flue, carries out desulfurization and denitrification reaction.
Preferably, the molar ratio of the amount of the straying quatity of sodium bicarbonate particle object and sulfur dioxide to be removed in stepb
Control is more than or equal to 2.1.
Preferably, it is additionally provided with desulfurization product recirculating system, straying quatity and titanium dioxide to be removed when sodium bicarbonate
The molar ratio of the amount of sulphur is greater than 2.1, runs the desulfurization product recirculating system in such a way that by-product recirculation volume is 20%.
A branch is drawn from bag filter bottom pneumatic ash conveying pipe, electric control valve, branch and system are provided in bypass line
Powder system feeding bin is connected, and the amount of desulfurization product in feeding bin is returned by electric control valve control loop.
Preferably, the reaction temperature in the step B is set as between 130~220 DEG C.
Preferably, the additional amount of dilute sulfuric acid in the step D is set as the pH value control of solution being about 7, and right
The solution carries out aerating oxidation processing, and wherein the residence time of aerating oxidation is not shorter than 2 minutes, and oxidation air coefficient is greater than
1.5。
Preferably, in the step E, 1 is pressed with sulfate ion in level-one mixed liquor and calcium bicarbonate: (1.05~
1.1) ratio is added in reaction kettle, and reaction time is not shorter than 2 hours.
Preferably, it in the step G, is added by with nitrate ion in three-level mixed liquor at the amount of 1: 1 molar ratio
Ammonium hydrogen carbonate.
Preferably, in the step H, the reaction temperature of crystallization treatment is controlled at 30 DEG C or so, and crystallization time was at 30 minutes
To 40 minutes.
Detailed description of the invention
Hereinafter, carrying out the embodiment that the present invention will be described in detail in conjunction with attached drawing, in which:
Fig. 1 shows the flow chart of two-part flue gas aftertreatment technology of the invention.
Description of symbols:
1, oxidant preparation system 2, denitration oxidative system
3, sodium bicarbonate storage and metering system 4, the powder system 5, desulphurization denitration absorption system
6, product recycling, transportation system 7, by-product dissolution filter system 8, byproduct reaction system
9, sodium bicarbonate purification system 10, Separation of gypsum system
Specific embodiment
In the following description, a large amount of concrete details are given so as to provide a more thorough understanding of the present invention.So
And it will be apparent to one skilled in the art that the embodiment of the present invention may not need one or more of these details
And it is carried out.In other examples, in order to avoid obscuring with the embodiment of the present invention, for well known in the art one
A little technical characteristics are not described.
In order to thoroughly understand the embodiment of the present invention, detailed structure will be proposed in following description.Obviously, of the invention
The execution of embodiment is not limited to the specific details that those skilled in the art is familiar with.Presently preferred embodiments of the present invention is detailed
Carefully it is described as follows, however other than these detailed descriptions, the present invention can also have other embodiments.
According to an aspect of the present invention, a kind of two-part flue gas aftertreatment technology is provided, wherein being shown in FIG. 1
Implement the equipment of the two-part flue gas aftertreatment technology.Specifically, which includes being connected to the denitration of e.g. coke oven flue
Oxidative system 2, the oxidant preparation system 1 that the oxidant of ozone or hydrogen peroxide etc. is sprayed into the denitration oxidative system,
Positioned at 2 downstream of denitration oxidative system for closing scrubbing CO_2 and nitrogen by spraying into sodium bicarbonate particle Internet of Things in flue
The desulphurization denitration absorption system 5 of oxide, for store and measure sodium bicarbonate sodium bicarbonate store and metering system 3 with
And by the sodium bicarbonate grind into powder from the system 3 and the powder system 4 of pneumatic conveying is carried out, is located in flue and is somebody's turn to do
Desulphurization denitration absorption system downstream, dedusting for intercepting and collecting the byproduct of reaction in flue gas and ash-transmission system 6, cigarette
Gas can be directly discharged into atmosphere after dedusting and ash-transmission system；Byproduct of reaction from dedusting and ash-transmission system 6 is defeated
It is sent to the solution that by-product dissolution forms reactant with filtration system 7, it is molten with filtration system 7 by being dissolved from by-product
The byproduct reaction system 8 that liquid is reacted with calcium bicarbonate obtains wherein purifying for the first time by Separation of gypsum system 10
Gypsum obtains ammonium nitrate solution and cold sodium bicarbonate solution through second of Crystallization Separation, by sodium bicarbonate solution via sodium bicarbonate
Purification system 9 obtains sodium bicarbonate powder, and the Powder Recovery is recycled to sodium bicarbonate storage and metering system 3,
It is thus achieved that the regeneration of fume treatment and by-product.
It will be described in detail two-part flue gas aftertreatment technology of the invention below, which includes cooperating type desulphurization denitration
Process section and sodium bicarbonate regeneration technology section, wherein the cooperating type desulfurizing and denitrifying process section the following steps are included:
Step A: oxidant is sprayed into realize to flue gas in flue with atomizing type in denitration oxidative system into flue
Contained in nitric oxide (NO) gaseous oxidation be nitrogen oxides；Specifically, the oxidant in step is
Come the ozone of autoxidator preparation system or 10% hydrogen peroxide, wherein the dosage of the oxidant is set as making in flue gas
Nitrogen dioxide and nitric oxide production molar ratio are greater than 1.In step A, wherein the reaction equation of the oxidizing NO is as follows:
3NO+O3→3NO2
H2O2→·OH
·OH+NO→NO2
NO+NO2→N2O3。
Step B: sodium bicarbonate particle object is sprayed into a manner of fine powder in system for desulfuration and denitration 5 into flue to realize pair
Sulfur dioxide contained in flue gas (SO2) and combining for the nitrogen oxides generated absorb to obtain comprising sodium sulphate, nitric acid in flue
Byproduct of reaction including sodium and sodium carbonate；The sodium bicarbonate particle object wherein sprayed into the system for desulfuration and denitration 5 into flue
Partial size at 20 μm or less.Specifically, sodium bicarbonate is initially stored in sodium bicarbonate storage and metering system 3, wherein should
Storage and metering system 3 are preferably the warehouse that a bottom is cone bucket form；Sodium bicarbonate raw material in the warehouse is through orlop
After star-shaped dust-discharging valve or screw(-type) feeder metering, it is added in graded impact mill and is ground to 20 μm or so partial sizes.Fine powder later
It is de- that the powder system 4 through all for example defeated powder blowers sprays into progress desulfurization in boiler or furnace flue in a manner of pneumatic conveying
Nitre reaction；Specifically, it is blown into flue as the sodium bicarbonate powder of desulfurizing agent, in for example, 130 DEG C or more temperature
Degree, sloughs carbon dioxide and water, forms microcellular structure on fine powder surface, quickly in flue gas sulfur dioxide SO2 and other are sour
Property gas reacts, and main net reaction is as follows:
2NaHCO3+SO2+1/2O2→Na2SO3+2CO2+H2O
Na2SO3+1/2O2→Na2SO4
2NaHCO3+SO3→Na2SO4+2CO2+H2O
NaHCO3+HCl→NaCl+CO2+H2O
NaHCO3+HF→NaF+CO2+H2O；
Further, nitrogen oxide NOx generated in SO2 and step A mutually promotes the reaction for absorbing and occurring such as in flue gas
Under:
SO32-+NO2+H2O→SO42-+2NO2-+2H+
NO2-+1/2O2→NO3-.Thus, it is possible to by flue gas sulfur dioxide and nitrogen oxides be separately converted to sulfuric acid
The byproducts of reaction such as sodium, sodium nitrate and sodium carbonate.Preferably, in order to guarantee the removal efficiency in flue gas, bicarbonate in stepb
The molar ratio control of the amount of the straying quatity of sodium particulate matter and sulfur dioxide to be removed is more than or equal to 2.1；Further preferably
Reaction temperature in the step B is set as between 130~220 DEG C by ground；It is further preferred that guaranteeing sodium bicarbonate
It is not shorter than 2 seconds reaction time between flue gas.
Step C: the flue gas containing above-mentioned reaction product is subjected to trapping processing by deduster, treated, and flue gas is discharged into
The byproduct of reaction of atmosphere, trapping is collected in by-product storehouse via ash-transmission system；Wherein pulsed cloth bag may be selected in deduster
Deduster or dry electrostatic cleaner.By-product is discharged to by-product storehouse into ash-transmission system after deduster traps after desulfurization
It is interior, and atmosphere can be directly discharged by removing purified neat stress.
The sodium bicarbonate regeneration technology section is carried out after flue gas removes after cooperating type desulfurizing and denitrifying process section, wherein
The sodium bicarbonate regeneration technology section includes:
Step D: the by-product collected in by-product storehouse is discharged into the by-product dissolution filter system of for example, dissolving tank
Solution is made, and is added into solution to consume the dilute sulfuric acid of the sodium carbonate in by-product to obtain sodium sulphate and sodium nitrate
Level-one mixed liquor；Preferably, be provided with aerating oxidation device in the reactor, and by the step D dilute sulfuric acid plus
Enter amount to be set as the control of the pH value of solution being about 7, and aerating oxidation processing is carried out to the solution, wherein aerating oxidation
Residence time is not shorter than 2 minutes, and oxidation air coefficient is greater than 1.5.
Step E: above-mentioned level-one mixed liquor is sent into the reactor of byproduct reaction system 8 and is carried out instead with calcium bicarbonate
It should be with the second level mixed liquor of obtained sodium bicarbonate, calcium sulfate and sodium nitrate；Preferably, it in the step E, is mixed with level-one
Sulfate ion and calcium bicarbonate are in 1 in liquid: the ratio of (1.05~1.1) is added in reactor, and reaction time is not shorter than
2 hours.
Step F: crystallization treatment is carried out to generate calcium sulphate dihydrate to second level mixed liquor, and is obtained after eddy flow is dehydrated
The gypsum isolated and the three-level mixed liquor by sodium bicarbonate and sodium nitrate；
Step G: ammonium hydrogen carbonate is added into three-level mixed liquor and is reacted so that the level Four of sodium bicarbonate and ammonium nitrate is made
Mixed liquor；Preferably, it in the step G, is added by with nitrate ion in three-level mixed liquor at the amount of 1: 1 molar ratio
Ammonium hydrogen carbonate.
Step H；Crystallization treatment is carried out to separate obtained sodium bicarbonate powder and ammonium nitrate to level Four mixed liquor.In the mistake
Cheng Zhong, by the way that, at 30 DEG C or so, crystallization time was at 30 minutes to 40 minutes, and carbonic acid is precipitated in crystallization first by solution temperature control
Hydrogen sodium suspension, the suspension generate sodium bicarbonate powder after sodium bicarbonate purification system 9 is dry, which is transmitted back to carbon
Sour hydrogen sodium storage and metering system 3 continue on for desulfurization and denitrification reaction.The ammonium nitrate solution isolated simultaneously is used as nitrogen fertilizer plant
Make fertile raw material.
By upper it is known that the present invention is absorbed using sodium bicarbonate powder and to be generated in SO2 reaction process in flue gas
The mechanism that Na2SO3 collaboration absorbs the NO after oxidation realizes simultaneous SO_2 and NO removal, and since SO2 and NOx collaboration absorbed
Absorption of mutually promoting in journey, desulfuration efficiency of the invention are higher than single using sodium bicarbonate powder in the prior art
Desulfuration efficiency when desulfurization.
Further, the product generated after technique desulphurization denitration of the invention is used as Na2SO4, NaNO3, NaNO2 and is lacked
The mixture of Na2CO3 is measured, the present invention is reacted to obtain gypsum and sodium bicarbonate and nitre using Ca (HCO3) 2 and NH4HCO3
Sour ammonium.Conventional by-product sodium bicarbonate and sulfuric acid small different from solubility curve difference in the prior art, separation is difficult
Ammonium, it is sodium bicarbonate and ammonium nitrate that the need in the present invention, which carry out the by-product of Crystallization Separation, and the two solubility curve difference is obvious
Increase, makes it possible to simply separate two kinds of substance crystallizations, to reduce construction investment cost.
It is illustrated in further detail below with reference to specific embodiment:
Embodiment 1
Pilot test platform is built in Tangshan coke-oven plant, flue gas used in pilot experiment is by coke-oven plant's coke oven
It produces the flue gas extraction a part generated during coke and carries out pilot plant test, drawn flue gas is after waste heat boiler cools down
Flue gas, by adjusting waste heat boiler come flue gas needed for obtaining the test under 130~200 DEG C of different temperatures.It is arranged simultaneously enough
Long flue, time needed for guaranteeing desulfurization and denitrification reaction.Bag filter is set, the product that reaction generates is collected place
Reason.Using liquid oxygen as oxygen source, ozone is generated using ozone generator, sprays into flue later and the NO in flue gas is aoxidized
Reaction.It is sprayed into flue after being ground using impact type graded mill to sodium bicarbonate raw material powder and carries out desulfurization and denitrification reaction.
By-product after collection enters regeneration unit, and it is de- that the sodium bicarbonate after regeneration sprays into progress desulfurization in flue after grinding machine is ground
Nitre absorbing reaction.SO2 concentration is 300mg/Nm3 or so, NOx 450mg/Nm3 in the exhaust gas that the coke oven generates.
The present embodiment involves the steps of:
By controlling the dosage of ozone, the amount of penetrating is that NO is all oxidized to NO2 in flue gas under theoretical calculation；Simultaneously
Grinding machine is controlled to control the grind size of fine powder at D90=20 μm；The amount of dusting is the straying quatity and removing SO2 of sodium bicarbonate
The molar ratio of amount is 3: 1.It is constant to control conditions above, change test flue-gas temperature used obtained under different smoke temperatures SO2 and
The removal efficiency of NOx, specific see Table 1 for details.
Table 1
Embodiment 2
Using pilot test platform used in embodiment 1, in the case where flue-gas temperature is 155 DEG C, the ozone amount of penetrating is theory
It calculates NO in lower flue gas and is all oxidized to NO2；The amount of dusting is the straying quatity of sodium bicarbonate and the molar ratio of the amount of removing SO2 is
2.1:1.Control conditions above is constant, changes the different grain size for generating fine powder for testing grinding machine milling used, has obtained different thin
The removal efficiency of SO2 and NOx under Powder Particle Size, specific see Table 2 for details.
Table 2
Embodiment 3
Using pilot test platform used in embodiment 1, in the case where flue-gas temperature is 155 DEG C；The amount of dusting is sodium bicarbonate
The molar ratio of the amount of straying quatity and removing SO2 is 2.1: 1, and the powder particle size of penetrating is D90≤20 μm.Control conditions above not
Become, adjust the power of ozone generator, change the dosage of ozone, has obtained the de- of SO2 and NOx under different NO oxidation ratios
Except efficiency, specific see Table 3 for details.
Table 3
The present invention has been explained by the above embodiments, but it is to be understood that, above-described embodiment is only intended to
The purpose of citing and explanation, is not intended to limit the invention to the scope of the described embodiments.Furthermore those skilled in the art
It is understood that the present invention is not limited to the above embodiments, introduction according to the present invention can also be made more kinds of member
Variants and modifications, all fall within the scope of the claimed invention for these variants and modifications.
Claims (10)
1. a kind of two-part flue gas aftertreatment technology, which is characterized in that the technique includes cooperating type desulfurizing and denitrifying process section and carbon
Sour hydrogen sodium regeneration technology section, wherein the cooperating type desulfurizing and denitrifying process section the following steps are included:
Step A: oxidant is sprayed into realize to nitric oxide contained in flue gas in flue (NO) with atomizing type into flue
Gaseous oxidation be nitrogen oxides；
Step B: sodium bicarbonate particle object is sprayed into a manner of fine powder into flue to realize to dioxy contained in flue gas in flue
The joint absorption for changing sulphur (SO2) and the nitrogen oxides generated is obtained comprising the reaction pair including sodium sulphate, sodium nitrate and sodium carbonate
Product；
Step C: carrying out trapping processing by deduster for the flue gas containing above-mentioned reaction product, and treated, and flue gas is discharged into atmosphere,
The byproduct of reaction of trapping is collected in by-product storehouse via ash-transmission system；
The sodium bicarbonate regeneration technology section is carried out after the removing of cooperating type desulfurizing and denitrifying process section in flue gas, wherein the bicarbonate
Sodium regeneration technology section includes:
Step D: the by-product collected in by-product storehouse being discharged into dissolving tank, solution be made, and is added into solution to consume
The dilute sulfuric acid of sodium carbonate in by-product is to obtain the level-one mixed liquor of sodium sulphate and sodium nitrate；
Step E: above-mentioned level-one mixed liquor is sent into reactor and is reacted with calcium bicarbonate sodium bicarbonate, calcium sulfate is made
With the second level mixed liquor of sodium nitrate；
Step F: crystallization treatment is carried out to generate calcium sulphate dihydrate to second level mixed liquor, and is isolated after eddy flow is dehydrated
Gypsum and three-level mixed liquor by sodium bicarbonate and sodium nitrate；
Step G: ammonium hydrogen carbonate is added into three-level mixed liquor and is reacted so that the mixing of the level Four of sodium bicarbonate and ammonium nitrate is made
Liquid；
Step H；Crystallization treatment is carried out to separate obtained sodium bicarbonate powder and ammonium nitrate to level Four mixed liquor.
2. two-part flue gas aftertreatment technology according to claim 1, which is characterized in that the oxygen in step
Agent is the hydrogen peroxide of ozone or 10%, wherein being set as making nitrogen dioxide and an oxidation in flue gas for the dosage of the oxidant
The molar ratio of nitrogen is greater than 1.
3. two-part flue gas aftertreatment technology according to claim 1, which is characterized in that sprayed in stepb into flue
The partial size of the sodium bicarbonate particle object entered is at 20 μm hereinafter, and through carrying out desulfurization and denitrification reaction in pneumatic conveying penetrating flue.
4. two-part flue gas aftertreatment technology according to claim 3, which is characterized in that sodium bicarbonate in stepb
The molar ratio control of the amount of the straying quatity and sulfur dioxide to be removed of grain object is more than or equal to 2.1.
5. two-part flue gas aftertreatment technology according to claim 4, which is characterized in that be additionally provided with desulfurization product and follow again
Loop system is recycled with by-product when the molar ratio of the amount of the straying quatity and sulfur dioxide to be removed of sodium bicarbonate is greater than 2.1
Amount runs the desulfurization product recirculating system for 20% mode.
6. two-part flue gas aftertreatment technology according to claim 1, which is characterized in that by the reaction in the step B
Temperature is set as between 130~220 DEG C.
7. two-part flue gas aftertreatment technology according to claim 1, it is characterised in that by dilute sulfuric acid in the step D
Additional amount is set as the control of the pH value of solution being about 7, and carry out aerating oxidation processing to the solution, wherein aerating oxidation
Residence time is not shorter than 2 minutes, and oxidation air coefficient is greater than 1.5.
8. two-part flue gas aftertreatment technology according to claim 1, which is characterized in that in the step E, with level-one
Sulfate ion and calcium bicarbonate are in 1 in mixed liquor: the ratio of (1.05~1.1) is added in reactor, and reaction time is not
Shorter than 2 hours.
9. the two-part flue gas aftertreatment technology according to claim 1, which is characterized in that in the step G,
Ammonium hydrogen carbonate is added at the amount of 1: 1 molar ratio by with nitrate ion in three-level mixed liquor.
10. two-part flue gas aftertreatment technology according to claim 1, which is characterized in that in the step H, at crystallization
The reaction temperature of reason is controlled at 30 DEG C or so, and crystallization time was at 30 minutes to 40 minutes.
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| CN113371735A (en) * | 2021-07-05 | 2021-09-10 | 浙江致远环境科技有限公司 | Process and device for producing anhydrous sodium sulphate by using sulfur dioxide in waste gas |
| CN114349028A (en) * | 2021-11-29 | 2022-04-15 | 攀钢集团研究院有限公司 | Method for resource utilization of vanadium precipitation wastewater |
| CN115893465A (en) * | 2022-11-28 | 2023-04-04 | 华南理工大学 | A waste salt recycling process |
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| CN115893465A (en) * | 2022-11-28 | 2023-04-04 | 华南理工大学 | A waste salt recycling process |
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Denomination of invention: A two-stage flue gas post-treatment process Granted publication date: 20220211 Pledgee: Bank of China Limited Beijing Shijingshan Branch Pledgor: BEIJING LIDEHENG ENVIRONMENTAL PROTECTION ENGINEERING Co.,Ltd. Registration number: Y2025980025100 |