CN110090538A - A kind of oxyradical wet process of FGD method of denitration - Google Patents
A kind of oxyradical wet process of FGD method of denitration Download PDFInfo
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Abstract
The invention proposes a kind of oxyradical wet process of FGD method of denitration, dedusting flue gas is sufficiently mixed after gas-gas heat exchanger cools down with misty hydrogen peroxide, and under the irradiation of ultraviolet light, generates a large amount of O3, the various actives free radical such as O, OH, hydrogen peroxide is by NOXIt is oxidized to NO2Or N2O3Or N2O5；Flue gas after aoxidizing therewith is sufficiently mixed with misty carbon ammonium aqueous solution, the sour gas such as oxysulfide and nitrogen oxides are once absorbed, enter the first gas-liquid separator afterwards, subsequent flue gas is reacted with misty fresh carbon ammonium aqueous solution again in subsequent pipeline, double absorption is carried out to sour gas such as oxysulfide remaining in flue gas and nitrogen oxides, secondary gas-liquid separation is carried out in the second gas-liquid separator afterwards, smoke backflow to gas-gas heat exchanger is discharged after heating up.The present invention effectively can remove oxysulfide and nitrogen oxides simultaneously, and the useful nitrogenous fertilizer of output improves the economy of desulphurization denitration, has many advantages, such as that easy to operate, at low cost, technical difficulty is small.
Description
Technical field
The present invention relates to environmental technology field more particularly to a kind of oxyradical wet process of FGD method of denitration.
Background technique
All exist in the every profession and trades such as thermal power plant, metallurgy, chemical industry, glass and contains a large amount of NOXAnd SO2Flue gas.It is common at present
The method of coordinated desulfurization denitrogenation have: copper oxide method, activated carbon method, calcium base absorption process, ferrous complex method, peroxide passivation, height
Potassium manganate soda solution grouting, liquor natrii hypochloritis's method, state of appraising at the current rate metal ion solution, photocatalysis oxidation technique and electro-catalytic oxidation technology
Deng.The processing scheme being now widely used in practice production is calcium base absorption process, mainly uses the desulfurization of calcium method, uses gaseous ammonia
NOX is reduced into nitrogen in SNCR or SCR technique.But the difficulty for the calcium sulfate waste residues processing that calcium method desulfurization generates is larger, city
Field is sold under pressure, and the environment on device periphery is poor, and SNCR or SCR technique uses ammonia or urea as reducing agent, no
Generate recyclable valuable product, the NO in flue gasXThe effective utilization of resources is not obtained.
Summary of the invention
Based on technical problem present in background technique, it is de- that the invention proposes a kind of oxyradical wet process of FGD
Nitre method.
A kind of oxyradical wet process of FGD method of denitration proposed by the present invention, comprising the following steps:
S1, dedusting flue gas is passed through in gas-gas heat exchanger cooling down, the dedusting flue gas after cooling is passed through in first pipe, and
SO in dedusting flue gas is detected by on-line checking device in first pipe2、NOXContent；
S2, it hydrogen peroxide is passed through in first pipe with atomised form is mixed with dedusting flue gas, while carrying out ultraviolet light,
Generate flue gas A；
S3, it carbon ammonium aqueous solution is passed through in first pipe with atomised form is mixed with flue gas A, generate flue gas B；
S4, flue gas B is passed through in the first gas-liquid separator, gas-liquid separation obtains flue gas C, and flue gas C is passed through second pipe
In；
S5, it carbon ammonium aqueous solution is passed through in second pipe is mixed with flue gas C, generate flue gas D；
S6, flue gas D is passed through in the second gas-liquid separator, gas-liquid separation obtains cleaning flue gases E, and cleaning flue gases E is by third
Pipeline is passed through in gas-gas heat exchanger and is discharged after heating.
Preferably, in S2, the concentration of hydrogen peroxide is 5-30wt%；Preferably, in S2, hydrogen peroxide concentration 7.5-
15wt%；Preferably, in S2, hydrogen peroxide is passed through in first pipe by the first delivery pump, multiple first atomizers；It is preferred that
, in S2, the quantity of the first atomizer is 1-10；It is furthermore preferred that the quantity of the first atomizer is 4-6.
Preferably, in S2, ultraviolet light is carried out by ultraviolet light generator；Preferably, in S2, ultraviolet light occurs
The quantity ratio of device and the first atomizer is 0.5-2；It is furthermore preferred that the quantity of ultraviolet light generator and the first atomizer ratio
Value is 1.
Preferably, in S3, the concentration of carbon ammonium aqueous solution is 0.5-30wt%；Preferably, in S3, carbon ammonium aqueous solution is dense
Degree is 5-10wt%；Preferably, in S3, carbon ammonium aqueous solution is passed through by the second delivery pump, multiple second atomizers
In one pipeline；Preferably, the quantity of the second atomizer is 1-10；It is furthermore preferred that the quantity of the second atomizer is 4-8
It is a.
Preferably, in S4, gas-liquid separation obtains liquid A, and liquid A is under centrifugal force and gravity in the first gas-liquid point
It is enriched with from device bottom and passes through pipeline to processing system.
Preferably, in S4, the first demister is added in second pipe and the first gas-liquid separator junction.
Preferably, in S5, the concentration of carbon ammonium aqueous solution is 0.5-30wt%.
Preferably, in S5, the carbon ammonium aqueous solution in surge tank is led to by third delivery pump, multiple third atomizers
Enter in second pipe；Preferably, the quantity of third atomizer is 1-8；It is furthermore preferred that the quantity of third atomizer is 2-
4.
Preferably, in S6, gas-liquid separation obtains liquid B, and liquid B is under centrifugal force and gravity in the second gas-liquid point
It is enriched with from device bottom and passes through pipeline to surge tank.
Preferably, in S6, the second demister is added in third pipeline and the second gas-liquid separator junction.
A kind of oxyradical wet process of FGD method of denitration proposed by the present invention, dedusting flue gas are dropped through gas-gas heat exchanger
Wen Hou is sufficiently mixed with misty hydrogen peroxide, and under the irradiation of ultraviolet light, generates a large amount of O3, the various actives such as O, OH from
By base, hydrogen peroxide is by NOXIt is oxidized to NO2Or N2O3Or N2O5；Flue gas and misty carbon ammonium aqueous solution after aoxidizing therewith is sufficiently mixed
It closes, the sour gas such as oxysulfide and nitrogen oxides is once absorbed, enter the first gas-liquid separator afterwards, liquid is enriched in
First gas-liquid separator bottom, is sent by pipeline to processing system；Subsequent flue gas is fresh with mist again in subsequent pipeline
Carbon ammonium aqueous solution reaction carries out double absorption to sour gas such as oxysulfide remaining in flue gas and nitrogen oxides, after the
Secondary gas-liquid separation is carried out in two gas-liquid separators, liquid is entered the buffer tank as an absorbent, smoke backflow to gas gas
It is discharged after heat exchanger heating.
Present invention process is simple, layout is convenient, is convenient for operation, is convenient for safeguarding, and hydrogen peroxide and carbon are added in first pipe
Atomization type sectional ejecting is used when ammonium salt solution, can not only be maintained longer time of contact, but also catalyst can be made uniform with flue gas
And reaction is come into full contact with, reach stable, efficient desulfurization removing nitric effect, while gas-liquid separation is carried out using gas-liquid separator, subtracts
Few land occupation, shortens process, and whole process is easy to operate, convenient for safeguarding；Oxidant and absorbent of the present invention can adjust automatically,
On-line checking device is set in one pipeline and third pipeline, according to the monitoring data of return, adjusts penetrating in real time using robot control system(RCS)
Hydrogen peroxide and carbon ammonium aqueous solution amount, avoid nitrogen oxides and SO2When excessively high, it is vented unqualified or nitrogen oxides and SO2
When too low, reagent is wasted；The present invention can be to avoid the escaping of ammonia, when using ammonia solution as absorbent, absorptivity and the escaping of ammonia rate
It is and to use ammonium bicarbonate the escaping of ammonia rate of one side ammonium bicarbonate can almost be ignored, another aspect carbon as absorbent there are contradictory
The solubility of ammonium can achieve 100g/100g water, can be configured to highly concentrated solution if necessary, and application range is wider, guarantee
Desulfurization effect；Material clear route of the present invention, explicitly point out flue gas, hydrogen peroxide, ammonium bicarbonate solution and absorb after solution source,
Circulation process and last whereabouts have integrality and operability, effectively can remove oxysulfide and nitrogen oxides simultaneously,
The useful nitrogenous fertilizer of output, improves the economy of desulphurization denitration, with easy to operate, at low cost, technical difficulty is small, maintenance side
Just, the advantages that without secondary pollution.
Detailed description of the invention
Fig. 1 is a kind of flow chart of oxyradical wet process of FGD method of denitration proposed by the present invention.
Specific embodiment
In the following, technical solution of the present invention is described in detail by specific embodiment.
Embodiment 1
As shown in Figure 1:
A kind of oxyradical wet process of FGD method of denitration proposed by the present invention, comprising the following steps:
S1, it dedusting flue gas is passed through in gas-gas heat exchanger 1 is cooled to 110 DEG C, total blast volume 5000Nm3/ h, after cooling
Dedusting flue gas is passed through in first pipe 2, and passes through SO in 3 dedusting flue gas of on-line checking device in first pipe 22Content is
4500mg/Nm3、NOXContent is 1200mg/Nm3；
S2, the 10wt% hydrogen peroxide of 74.5kg/h is passed through the first pipe by 4,4 the first atomizers 5 of the first delivery pump
It is mixed in road 2 with dedusting flue gas, and under the ultraviolet light that 4 high-pressure sodium lamps 6 generate, generates flue gas A, flue gas A contains greatly
The O of amount3, various actives free radical and NO, the N such as O, OH2O3、N2O5；
S3, the 10wt% carbon ammonium aqueous solution of 480kg/h in surge tank 11 is passed through into 7, the 4 second atomization sprays of the second delivery pump
First 8, which are passed through in first pipe 2 flue gas A, mixes, in flue gas A oxysulfide and the sour gas such as nitrogen oxides once inhaled
It receives, generates flue gas B；
S4, the flue gas B after removal sour gas is passed through in the first gas-liquid separator 9, gas-liquid separation obtains flue gas C and liquid
Flue gas C is passed through in second pipe 10 by body A by demister 12, and liquid A is under centrifugal force and gravity in the first gas-liquid point
It is enriched with from 9 bottom of device and passes through pipeline to processing system；
S5, the fresh carbon ammonium aqueous solution of the 10wt% of 480kg/h is passed through into 12,2 third atomizers 13 of third delivery pump
It is passed through in second pipe 10 and is mixed with flue gas C, by the acidity such as the unabsorbed oxysulfide of small part and nitrogen oxides in flue gas C
Gas carries out double absorption, generates flue gas D；
S6, flue gas D is passed through in the second gas-liquid separator 14, gas-liquid separation obtains cleaning flue gases E and liquid B, cleans cigarette
Gas E is passed through in gas-gas heat exchanger 1 by third pipeline 16 by the second demister 15 and is discharged after heating, and the flue gas utilization of discharge is online
Detector 17 measures SO2Content is 30mg/Nm3, NOXContent is 17mg/Nm3, meet minimum discharge requirement, liquid B is in centrifugal force
Be enriched under gravity in 15 bottom of the second gas-liquid separator and pass through the 4th pipeline to surge tank 11.
Embodiment 2
As shown in Figure 1:
A kind of oxyradical wet process of FGD method of denitration proposed by the present invention, comprising the following steps:
S1, it dedusting flue gas is passed through in gas-gas heat exchanger 1 is cooled to 100 DEG C, total blast volume 10000Nm3/ h, after cooling
Dedusting flue gas is passed through in first pipe 2, and passes through SO in 3 dedusting flue gas of on-line checking device in first pipe 22Content is
3500mg/Nm3、NOXContent is 1000mg/Nm3；
S2, the 7.5wt% hydrogen peroxide of 167kg/h is passed through the first pipe by 4,6 the first atomizers 5 of the first delivery pump
It is mixed in road 2 with dedusting flue gas, and under the ultraviolet light that 6 high-pressure sodium lamps 6 generate, generates flue gas A, flue gas A contains greatly
The O of amount3, various actives free radical and NO, the N such as O, OH2O3、N2O5；
S3, the 5wt% carbon ammonium aqueous solution of 1380kg/h in surge tank 11 is passed through into 7, the 6 second atomization sprays of the second delivery pump
First 8, which are passed through in first pipe 2 flue gas A, mixes, in flue gas A oxysulfide and the sour gas such as nitrogen oxides once inhaled
It receives, generates flue gas B；
S4, the flue gas B after removal sour gas is passed through in the first gas-liquid separator 9, gas-liquid separation obtains flue gas C and liquid
Flue gas C is passed through in second pipe 10 by body A by demister 12, and liquid A is under centrifugal force and gravity in the first gas-liquid point
It is enriched with from 9 bottom of device and passes through pipeline to processing system；
S5, the fresh carbon ammonium aqueous solution of the 5wt% of 690kg/h is led to by 12,3 third atomizers 13 of third delivery pump
Enter and mixed in second pipe 10 with flue gas C, by the sour gas such as the unabsorbed oxysulfide of small part and nitrogen oxides in flue gas C
Body carries out double absorption, generates flue gas D；
S6, flue gas D is passed through in the second gas-liquid separator 14, gas-liquid separation obtains cleaning flue gases E and liquid B, cleans cigarette
Gas E is passed through in gas-gas heat exchanger 1 by third pipeline 16 by the second demister 15 and is discharged after heating, and the flue gas utilization of discharge is online
Detector 17 measures SO2Content is 28mg/Nm3, NOXContent is 21mg/Nm3, meet minimum discharge requirement, liquid B is in centrifugal force
Be enriched under gravity in 15 bottom of the second gas-liquid separator and pass through the 4th pipeline to surge tank 11.
Embodiment 3
As shown in Figure 1:
A kind of oxyradical wet process of FGD method of denitration proposed by the present invention, comprising the following steps:
S1, it dedusting flue gas is passed through in gas-gas heat exchanger 1 is cooled to 90 DEG C, total blast volume 15000Nm3/ h, after cooling
Dedusting flue gas is passed through in first pipe 2, and passes through SO in 3 dedusting flue gas of on-line checking device in first pipe 22Content is
3000mg/Nm3、NOXContent is 800mg/Nm3；
S2, the 15wt% hydrogen peroxide of 100kg/h is passed through the first pipe by 4,5 the first atomizers 5 of the first delivery pump
It is mixed in road 2 with dedusting flue gas, and under the ultraviolet light that 5 high-pressure sodium lamps 6 generate, generates flue gas A, flue gas A contains greatly
The O of amount3, various actives free radical and NO, the N such as O, OH2O3、N2O5；
S3, the 7.5wt% carbon ammonium aqueous solution of 1280kg/h in surge tank 11 is passed through into the second delivery pump 7,8 second atomizations
Spray head 8 is passed through in first pipe 2 flue gas A and mixes, in flue gas A oxysulfide and the sour gas such as nitrogen oxides carry out it is primary
It absorbs, generates flue gas B；
S4, the flue gas B after removal sour gas is passed through in the first gas-liquid separator 9, gas-liquid separation obtains flue gas C and liquid
Flue gas C is passed through in second pipe 10 by body A by demister 12, and liquid A is under centrifugal force and gravity in the first gas-liquid point
It is enriched with from 9 bottom of device and passes through pipeline to processing system；
S5, the fresh carbon ammonium aqueous solution of the 7.5wt% of 1280kg/h is passed through into 12,4 third atomizers of third delivery pump
13 are passed through in second pipe 10 and mix with flue gas C, by the acid such as the unabsorbed oxysulfide of small part and nitrogen oxides in flue gas C
Property gas carry out double absorption, generate flue gas D；
S6, flue gas D is passed through in the second gas-liquid separator 14, gas-liquid separation obtains cleaning flue gases E and liquid B, cleans cigarette
Gas E is passed through in gas-gas heat exchanger 1 by third pipeline 16 by the second demister 15 and is discharged after heating, and the flue gas utilization of discharge is online
Detector 17 measures SO2Content is 32mg/Nm3, NOXContent is 23mg/Nm3, meet minimum discharge requirement, liquid B is in centrifugal force
Be enriched under gravity in 15 bottom of the second gas-liquid separator and pass through the 4th pipeline to surge tank 11.
The foregoing is only a preferred embodiment of the present invention, but scope of protection of the present invention is not limited thereto,
Anyone skilled in the art in the technical scope disclosed by the present invention, according to the technique and scheme of the present invention and its
Inventive concept is subject to equivalent substitution or change, should be covered by the protection scope of the present invention.
Claims (10)
1. a kind of oxyradical wet process of FGD method of denitration, which comprises the following steps:
S1, dedusting flue gas is passed through in gas-gas heat exchanger cools down, the dedusting flue gas after cooling is passed through in first pipe, and first
SO in dedusting flue gas is detected by on-line checking device in pipeline2、NOXContent；
S2, it hydrogen peroxide is passed through in first pipe with atomised form is mixed with dedusting flue gas, while carrying out ultraviolet light, generated
Flue gas A；
S3, it carbon ammonium aqueous solution is passed through in first pipe with atomised form is mixed with flue gas A, generate flue gas B；
S4, flue gas B is passed through in the first gas-liquid separator, gas-liquid separation obtains flue gas C, and flue gas C is passed through in second pipe；
S5, it carbon ammonium aqueous solution is passed through in second pipe is mixed with flue gas C, generate flue gas D；
S6, flue gas D is passed through in the second gas-liquid separator, gas-liquid separation obtains cleaning flue gases E, and cleaning flue gases E is by third pipeline
It is passed through after heating up in gas-gas heat exchanger and is discharged.
2. oxyradical wet process of FGD method of denitration according to claim 1, which is characterized in that double in S2
The concentration of oxygen water is 5-30wt%；Preferably, in S2, hydrogen peroxide concentration 7.5-15wt%；Preferably, in S2, dioxygen
Water is passed through in first pipe by the first delivery pump, multiple first atomizers；Preferably, in S2, the first atomizer
Quantity is 1-10；It is furthermore preferred that the quantity of the first atomizer is 4-6.
3. oxyradical wet process of FGD method of denitration according to claim 1, which is characterized in that in S2, lead to
It crosses ultraviolet light generator and carries out ultraviolet light；Preferably, in S2, the quantity ratio of ultraviolet light generator and the first atomizer
Value is 0.5-2；It is furthermore preferred that the quantity ratio of ultraviolet light generator and the first atomizer is 1.
4. oxyradical wet process of FGD method of denitration according to any one of claim 1-3, which is characterized in that
In S3, the concentration of carbon ammonium aqueous solution is 0.5-30wt%；Preferably, in S3, carbon ammonium aqueous solution concentration is 5-10wt%；It is excellent
Choosing, in S3, the carbon ammonium aqueous solution in surge tank is passed through first pipe by the second delivery pump, multiple second atomizers
It is interior；Preferably, the quantity of the second atomizer is 1-10；It is furthermore preferred that the quantity of the second atomizer is 4-8.
5. oxyradical wet process of FGD method of denitration according to any one of claim 1-3, which is characterized in that
In S4, gas-liquid separation obtains liquid A, and liquid A is enriched with simultaneously under centrifugal force and gravity in the first gas-liquid separator bottom
Pass through pipeline to processing system.
6. oxyradical wet process of FGD method of denitration according to any one of claim 1-3, which is characterized in that
In S4, the first demister is added in second pipe and the first gas-liquid separator junction.
7. oxyradical wet process of FGD method of denitration according to any one of claim 1-3, which is characterized in that
In S5, the concentration of carbon ammonium aqueous solution is 0.5-30wt%.
8. oxyradical wet process of FGD method of denitration according to any one of claim 1-3, which is characterized in that
In S5, carbon ammonium aqueous solution is passed through in second pipe by third delivery pump, multiple third atomizers；Preferably, third
The quantity of atomizer is 1-8；It is furthermore preferred that the quantity of third atomizer is 2-4.
9. oxyradical wet process of FGD method of denitration according to claim 8, which is characterized in that in S6, gas
The isolated liquid B of liquid, liquid B is enriched under centrifugal force and gravity in the second gas-liquid separator bottom and to pass through pipeline defeated
It send to surge tank.
10. oxyradical wet process of FGD method of denitration according to any one of claim 1-3, feature exist
In adding the second demister in third pipeline and the second gas-liquid separator junction in S6.
Priority Applications (1)
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