CN107661693A - A kind of method and combined system of the flue gas denitrification system stable operations of SCR in low- load conditions - Google Patents
A kind of method and combined system of the flue gas denitrification system stable operations of SCR in low- load conditions Download PDFInfo
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- CN107661693A CN107661693A CN201610604979.2A CN201610604979A CN107661693A CN 107661693 A CN107661693 A CN 107661693A CN 201610604979 A CN201610604979 A CN 201610604979A CN 107661693 A CN107661693 A CN 107661693A
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- flue gas
- adsorbent
- scr
- gas denitrification
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- 239000003546 flue gas Substances 0.000 title claims abstract description 90
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 87
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000003463 adsorbent Substances 0.000 claims abstract description 43
- 239000002245 particle Substances 0.000 claims abstract description 19
- 239000003513 alkali Substances 0.000 claims abstract description 18
- 238000002347 injection Methods 0.000 claims abstract description 11
- 239000007924 injection Substances 0.000 claims abstract description 11
- 239000000843 powder Substances 0.000 claims abstract description 10
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical group [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 10
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 claims description 3
- 239000001095 magnesium carbonate Substances 0.000 claims description 3
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims description 3
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 3
- 239000000347 magnesium hydroxide Substances 0.000 claims description 3
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 2
- 239000000920 calcium hydroxide Substances 0.000 claims description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 2
- QWDJLDTYWNBUKE-UHFFFAOYSA-L magnesium bicarbonate Chemical compound [Mg+2].OC([O-])=O.OC([O-])=O QWDJLDTYWNBUKE-UHFFFAOYSA-L 0.000 claims 2
- 239000002370 magnesium bicarbonate Substances 0.000 claims 2
- 229910000022 magnesium bicarbonate Inorganic materials 0.000 claims 2
- 235000014824 magnesium bicarbonate Nutrition 0.000 claims 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims 1
- 239000011575 calcium Substances 0.000 claims 1
- 229910052791 calcium Inorganic materials 0.000 claims 1
- 239000001301 oxygen Substances 0.000 claims 1
- 229910052760 oxygen Inorganic materials 0.000 claims 1
- 239000002250 absorbent Substances 0.000 abstract description 10
- 230000002745 absorbent Effects 0.000 abstract description 10
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 35
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 19
- 239000003054 catalyst Substances 0.000 description 16
- 239000002585 base Substances 0.000 description 10
- 239000007789 gas Substances 0.000 description 10
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 6
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- WWILHZQYNPQALT-UHFFFAOYSA-N 2-methyl-2-morpholin-4-ylpropanal Chemical compound O=CC(C)(C)N1CCOCC1 WWILHZQYNPQALT-UHFFFAOYSA-N 0.000 description 5
- 235000011130 ammonium sulphate Nutrition 0.000 description 5
- 235000019504 cigarettes Nutrition 0.000 description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 230000000903 blocking effect Effects 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000010881 fly ash Substances 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 241001625808 Trona Species 0.000 description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000000178 monomer Substances 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000000908 ammonium hydroxide Substances 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 238000005422 blasting Methods 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- 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
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
- B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
-
- 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
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Dispersion Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of method of the flue gas denitrification system stable operations of SCR in low- load conditions, it is characterized in that, injection system is respectively arranged before and after SCR flue gas denitrification systems, for being blown nanoscale dry powder alkali formula adsorbent into flue gas, the particle diameter of the absorbent particles is 5 100nm.The invention also discloses a kind of denitrating flue gas combined system of stable operation in low- load conditions.
Description
Technical field
The present invention relates to a kind of method and combined system of the flue gas denitrification system stable operations of SCR in low- load conditions.
Background technology
In order to remove the nitrogen oxides in combustion product gases, prevent from polluting environment, it is necessary to carry out denitration process to combustion product gases.
At present, the denitration technology industrially commonly used is SCR technology (SCR), its restoring function using ammonia to NOx,
NOx (mainly NO) is reduced to be not much air the N of influence in the presence of catalyst2And water, reducing agent NH3。
It should be noted that in coal-fired flue-gas, sulphur content is contained in fuel, contains substantial amounts of dioxy in caused flue gas
Change sulphur and a small amount of sulfur trioxide.It is sulfur trioxide that SCR flue gas denitrification systems, which cause this part sulfur dioxide inverted, in spray ammoniacal liquor
After form acid mist, while with the NH of excess3Ammonium sulfate and ammonium hydrogen sulfate are generated, these directly results in the blocking of air preheater with after
End equipment is corroded.In addition, ammonium sulfate and the micropore on ammonium hydrogen sulfate meeting blocking catalyst surface, make catalyst failure, reduce SCR
The efficiency of flue gas denitrification system, reduce the service life of catalyst.The sulfur trioxide discharged after SCR flue gas denitrification systems can be right
Atmospheric environment causes serious pollution.
US7618602, US6126910, US6803025 disclose the solution that alkaline matter is sprayed into flue gas.
US6126910 sprays into the solution containing bisulfite into flue gas, and US6803025 sprays into sodium carbonate, bicarbonate into flue gas
Sodium, sodium hydroxide, ammonium hydroxide, potassium hydroxide, the solution of potassium carbonate and saleratus, but the content base of sulfur dioxide in flue gas
This is not reduced.
CN103055684A discloses a kind of device and technique that sulfur trioxide in flue gas is effectively removed using trona,
Nozzle system is set at the flue between SCR reactors afterbody and air preheater, trona slurries are sprayed into flue.
Subject matter existing for the above method of the prior art is drop atomization technique, and the technology realizes condition at present
Harshness, technical costs are higher.
This invention address that a kind of method of flue gas denitrification system stable operations of SCR in low- load conditions is provided and is
System, the efficiency of SCR flue gas denitrification systems under underload (≤50%) operating mode can be optimized, reduce the pollutant in discharge flue gas.
The content of the invention
The present invention provides a kind of method of the flue gas denitrification system stable operations of SCR in low- load conditions, it is characterised in that
Injection system is respectively arranged before and after SCR flue gas denitrification systems, for being blown nanoscale dry powder alkali formula adsorbent into flue gas.
Using the method for the present invention, the SCR flue gas denitrification systems under underload (≤50%) operating mode can be greatly lowered
The middle possibility blocked because forming ABS and ammonium hydrogen sulfate, the denitration efficiency of SCR flue gas denitrification systems is improved, is extended
The service life of catalyst, it is cost-effective, so as to ensure that the normal operation of SCR flue gas denitrification systems, while prevent
The stickum such as ammonium sulfate and ammonium hydrogen sulfate blocks boiler air preheater and rear end equipment, has ensured the steady of overall flue system
Fixed operation.
The present invention also provides a kind of denitrating flue gas combined system of stable operation in low- load conditions, and it includes SCR cigarettes
Gas denitrating system and injection system, it is characterised in that be respectively arranged before and after SCR flue gas denitrification systems for being sprayed into flue gas
Shot blasting footpath is the injection system of 5-100nm nanoscale dry powder alkali formula adsorbent.
Brief description of the drawings
Fig. 1 shows the schematic diagram of the denitrating flue gas combined system of the present invention.
Fig. 2 is shown under different boiler working conditions, using alkali formula adsorbent with being blown without using alkali formula adsorbent, SCR
The change of the denitration efficiency of flue gas denitrification system.
Fig. 3 is shown under the conditions of different boiler working conditions, is blown the absorbent particles of different-grain diameter, SCR denitrating flue gas system
The contrast of the denitration efficiency of system.
Fig. 4 shown under different working conditions, different adsorbents：SO3The denitration of SCR flue gas denitrification systems under mol ratio
Efficiency.
Fig. 5 shows boiler under 50% load, Xi Fu Ji ︰ SO3Mol ratio is 8:When 1, adsorbent different time is blown
The denitration efficiency of SCR flue gas denitrification systems afterwards.
Embodiment
SCR flue gas denitrification systems used in the method for the present invention can be SCR denitrating flue gas as known in the art
System.
Injection system used in the method for the present invention can be injection system as known in the art.
In a preferred embodiment of the invention, adsorbent used is selected from sodium base adsorbent, Ca-base adsorbent, magnesium-based and inhaled
Common base adsorbent in this area such as attached dose, it is specially：Sodium carbonate, sodium acid carbonate, calcium hydroxide, magnesium carbonate, bicarbonate
The one or more therein such as magnesium, magnesium hydroxide.The adsorbent can be used alone or in combination, as long as not influenceing as absorption
The performance of agent.
In a preferred embodiment of the invention, the particle diameter of absorbent particles used is 5-100nm, preferably 10-
50nm, specific surface area 65-90m2/g。
The specific surface area of the absorbent particles of the present invention is big, and aperture is small, adsorption capacity is high, reaction rate is fast, cost is not high,
Physico-chemical property is similar with flyash, does not influence continuing with for boiler dust removal system and the original flyash of power plant.
The dry powder alkali formula adsorbent in flue with SO2、SO3、H2SO4Gas-solid reaction occurs rapidly Deng gas, can be in cigarette
Reacted rapidly below 300 DEG C of temperature degree, generate sulfate solid, do not produce new harmful side product, can enter with flying dust
Subordinate equipment.To SO2、SO3、H2SO4SCR flue gas denitrification systems and pot is greatly lowered up to more than 90% in adsorption rate Deng gas
The generation that stove air preheater blocks, improves the denitration efficiency of SCR flue gas denitrification systems and the heat exchange efficiency of air preheater,
Extend conventional catalyst service life.
By arranging injection system before SCR flue gas denitrification systems, reduce sulfur dioxide and sulfur trioxide in flue gas,
Avoid and produce ammonium sulfate and ammonium hydrogen sulfate in SCR flue gas denitrification systems and damaged to caused by SCR flue gas denitrification systems, carry
The high denitration efficiency of SCR flue gas denitrification systems.
Dry powder alkali formula adsorbent is blown before SCR flue gas denitrification systems, adsorbs the SO in flue gas2、SO3Deng sour gas,
Avoid this partially acidic gas and NH excessive in flue3Reaction, the adhesive attachment thing of hydrogen sulfate ammonia and ammonium sulfate is formed, it is attached
In catalyst surface, blocking catalyst micropore, reduce catalyst denitration efficiency and shorten the service life of catalyst.
By arranging injection system after boiler SCR flue gas denitrification systems, reduce further in SCR flue gas denitrification systems
Middle SO2/SO3Conversion ratio, reduce the yield of sulfur trioxide, reduce sour gas and environment is polluted.
The adsorbent is blown in SCR flue gas denitrification systems exit, is adsorbed caused one in SCR flue gas denitrification systems
Part SO3Deng sour gas, avoid the sticky products such as ammonium sulfate, hydrogen sulfate ammonia from blocking and corrode air preheater, dust arrester etc.
Subordinate equipment, can the subordinate equipment such as exhaust air preheater, dust arrester operating efficiency and service life.
Those skilled in the art can by determining the content of sulfur dioxide and sulfur trioxide in flue gas, concrete decision to
The amount of base adsorbent is sprayed into flue gas.
When nanoscale alkali formula adsorbent is blown after SCR flue gas denitrification systems, adsorbent：SO3Mol ratio is 4:1 to 8:1
In the range of.
Due to the seasonal variation of power consumption, power plant's generated energy under different operating modes is different, causes smoke temperature change width
Degree is very big, and in SCR flue gas denitrification systems, influence of the flue-gas temperature to catalyst is huge.When boiler at low load operates, cigarette
Temperature degree drops to less than 300 DEG C, and the reactivity of denitrating catalyst substantially reduces at this temperature, causes the de- of denitrating catalyst
Nitre efficiency degradation, then have impact on boiler of power plant NOx discharge, environment is damaged.Usually need in the prior art
Flue gas is heated in favor of SCR flue gas denitrification system normal operations.
The method of the present invention is simultaneously suitable for caused flue gas under power plant's high load capacity operating mode and running on the lower load.
Using the method for the present invention, the normal operation of SCR flue gas denitrification systems can be ensured under power plant's full working scope, made
The denitration rate of SCR flue gas denitrification systems reaches newest national requirements for environmental protection, SO2/SO3<1%, SO3Discharge capacity Deng gas reduces
To below 3ppm.
Embodiment
The present invention is further described below in conjunction with accompanying drawing.
Fig. 1 shows the schematic diagram of the denitrating flue gas combined system of the present invention.According to Fig. 1, before SCR flue gas denitrification systems
Nozzle is set respectively with rear, for spraying into dry powder base adsorbent into flue gas.
Analog flue gas experiment is carried out in laboratory, and with blowing into certain flyash.In SCR flue gas denitrification systems
With NO concentration detection apparatus, SO are set respectively before air preheater3Gas concentration detection apparatus, SO2Gas concentration detection apparatus,
According to NO, SO of disengaging SCR flue gas denitrification systems3、SO2Gas concentration calculates the SO of catalyst2/SO3Conversion ratio and denitration effect
Rate.
The composition of analog flue gas is as follows：
NO contents：500mg/Nm3 O2Content：5%
SO3Content：6mg/Nm3 SO2Content：650mg/Nm3
H2O content：10%
Catalyst experiment monomer parameter list is as shown in table 1 below.
Catalyst monomer specification is used in the experiment of table 1
Using 0.3-0.6MPa compressed air spraying nanoscale (5-100nm) base adsorbent, sprayed through bimetal wear resistant
Mouth is blown into flue.It is blown the base adsorbent of different-grain diameter respectively under different operating modes.Contrived experiment is as follows：
Embodiment 1：Under boiler difference working condition, SCR flue gas denitrification systems before and after 10nm particle diameter alkali formula adsorbents are blown
Denitration efficiency contrast.
Nanoscale alkali formula absorbent particles with compressed air enter flue in, rapidly with the SO in flue gas2、SO3、H2SO4Deng
Gas-solid reaction occurs for sour gas, generation sulfate, the solid granule of sulphite, enters subordinate equipment with cigarette ash.
Fig. 2 is shown under different boiler working conditions (entering cigarette temperature), is blown alkali formula adsorbent and is not blown alkali formula adsorbent,
The change of the denitration efficiency of SCR flue gas denitrification systems.
It can be observed from fig. 2 that the base absorbent particles of the present invention have substantially to the denitration efficiency of SCR flue gas denitrification systems
Under facilitation, particularly boiler at low load operating mode, when flue-gas temperature is below 300 DEG C, raising efficiency becomes apparent.
Embodiment 2：Under boiler difference working condition, different-grain diameter 10nm, 30nm, 50nm absorbent particles are blown.
Fig. 3 is shown under the conditions of different boiler working conditions, is blown the absorbent particles of different-grain diameter, SCR denitrating flue gas system
The contrast of the denitration efficiency of system.
As seen from Figure 3, the base absorbent particles of 15nm, 30nm and 50nm particle diameter are to lifting SCR denitrating flue gas system
The denitration efficiency of system has a positive effect, and enhancing rate difference is less big.
Embodiment 3：Under different working conditions, nanoscale alkali formula adsorbent, difference absorption are blown after SCR flue gas denitrification systems
Agent：SO3Mol ratio.
Fig. 4 is shown under different working conditions, and nanoscale alkali formula adsorbent, absorption are blown after SCR flue gas denitrification systems
Agent：SO3Mol ratio is respectively 4:1、6:1、8:When 1, the denitration efficiency of SCR flue gas denitrification systems.
From fig. 4 it can be seen that mol ratio is 8:When 1, the effect for being blown absorbent particles is best.
Embodiment 4：Under the loading condiction of boiler 50%, adsorbent：SO3Mol ratio is 8:When 1, adsorbent is blown 1 minute-
140 minutes.
Fig. 5 shows boiler under 50% loading condiction, adsorbent：SO3Mol ratio is 8:When 1, injection adsorbent is different
The change of the denitration efficiency of SCR flue gas denitrification systems after time.
Fig. 5 shown after adsorbent is blown, the effect of SCR flue gas denitrification systems out of 1 minute -140 minutes continuous times
The change of rate.Fig. 5 shows that the efficiency of SCR flue gas denitrification systems can be stablized adsorbent in 1 hour after flue is entered.
The embodiment of the present invention is described above in association with accompanying drawing, but the present invention is not limited thereto.Not
In the range of the purport of the present invention, those skilled in the art can enter to specific embodiments of the present invention described here
Row changes and equivalent transformation, but these should be considered as within claimed the scope of the present invention.
Claims (10)
- A kind of 1. method of the flue gas denitrification system stable operations of SCR in low- load conditions, it is characterised in that taken off in SCR flue gases Injection system is respectively arranged before and after nitre system, for being blown nanoscale dry powder alkali formula adsorbent, the adsorbent into flue gas The particle diameter of particle is 5-100nm.
- 2. the method as described in claim 1, it is characterised in that the running on the lower load is the temperature of flue gas below 300 DEG C Operating mode.
- 3. method as claimed in claim 1 or 2, it is characterised in that the adsorbent is selected from sodium carbonate, sodium acid carbonate, hydrogen-oxygen Change the one or more in calcium, magnesium carbonate, magnesium bicarbonate and magnesium hydroxide.
- 4. method as claimed in claim 1 or 2, it is characterised in that be blown adsorbent after SCR flue gas denitrification systems：SO3Rub That ratio is 4:1 to 8:Nanoscale dry powder alkali formula adsorbent in the range of 1.
- 5. method as claimed in claim 1 or 2, it is characterised in that the particle diameter of the adsorbent is 10-50nm.
- 6. a kind of denitrating flue gas combined system of stable operation in low- load conditions, it includes SCR flue gas denitrification systems and spray Blow system, it is characterised in that it is 5-100nm to be respectively arranged before and after SCR flue gas denitrification systems for being blown particle diameter into flue gas Nanoscale dry powder alkali formula adsorbent injection system.
- 7. combined system as claimed in claim 6, it is characterised in that the running on the lower load is the temperature of flue gas at 300 DEG C Following operating mode.
- 8. combined system as claimed in claims 6 or 7, it is characterised in that the adsorbent be selected from sodium carbonate, sodium acid carbonate, One or more in calcium hydroxide, magnesium carbonate, magnesium bicarbonate and magnesium hydroxide.
- 9. combined system as claimed in claims 6 or 7, it is characterised in that be blown adsorbent after SCR flue gas denitrification systems： SO3Mol ratio is 4:1 to 8:Nanoscale dry powder alkali formula adsorbent in the range of 1.
- 10. combined system as claimed in claims 6 or 7, it is characterised in that the particle diameter of the adsorbent is 10-50nm.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2023040132A1 (en) * | 2021-09-15 | 2023-03-23 | 黄庆华 | System for reducing blockages of ammonium bisulfate in air preheater of coal-fired power station |
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