CN108176204A - Flue gas and desulfurizing and denitrifying integrated purification system and purification method - Google Patents
Flue gas and desulfurizing and denitrifying integrated purification system and purification method Download PDFInfo
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- CN108176204A CN108176204A CN201711437385.8A CN201711437385A CN108176204A CN 108176204 A CN108176204 A CN 108176204A CN 201711437385 A CN201711437385 A CN 201711437385A CN 108176204 A CN108176204 A CN 108176204A
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- Prior art keywords
- flue gas
- fluidized bed
- recirculating fluidized
- gas
- desulfurizing
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- 239000003546 flue gas Substances 0.000 title claims abstract description 117
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 112
- 230000003009 desulfurizing Effects 0.000 title claims abstract description 67
- 238000000746 purification Methods 0.000 title claims abstract description 29
- 230000003134 recirculating Effects 0.000 claims abstract description 53
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 45
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 35
- 239000007921 spray Substances 0.000 claims abstract description 30
- 239000007787 solid Substances 0.000 claims abstract description 29
- UIIMBOGNXHQVGW-UHFFFAOYSA-M NaHCO3 Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 24
- 239000006096 absorbing agent Substances 0.000 claims abstract description 14
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims abstract description 12
- 235000017557 sodium bicarbonate Nutrition 0.000 claims abstract description 12
- 239000000843 powder Substances 0.000 claims description 43
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 31
- 239000000428 dust Substances 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 23
- 239000002994 raw material Substances 0.000 claims description 12
- 239000000779 smoke Substances 0.000 claims description 9
- 239000000126 substance Substances 0.000 claims description 7
- 239000002699 waste material Substances 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 239000003245 coal Substances 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- 229910052791 calcium Inorganic materials 0.000 claims description 5
- 230000000149 penetrating Effects 0.000 claims description 5
- 230000001133 acceleration Effects 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 3
- 239000011734 sodium Substances 0.000 claims description 3
- 229910052708 sodium Inorganic materials 0.000 claims description 3
- 230000000875 corresponding Effects 0.000 claims description 2
- 238000005243 fluidization Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims 1
- 238000009736 wetting Methods 0.000 claims 1
- 238000005245 sintering Methods 0.000 abstract description 12
- 229910000831 Steel Inorganic materials 0.000 abstract description 11
- 239000010959 steel Substances 0.000 abstract description 11
- 239000006227 byproduct Substances 0.000 abstract description 3
- 238000004140 cleaning Methods 0.000 abstract description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 16
- 238000005516 engineering process Methods 0.000 description 14
- PMZURENOXWZQFD-UHFFFAOYSA-L na2so4 Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 12
- 239000003570 air Substances 0.000 description 11
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium monoxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 9
- VWDWKYIASSYTQR-UHFFFAOYSA-N Sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 8
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 7
- 239000011575 calcium Substances 0.000 description 7
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 6
- 229910052938 sodium sulfate Inorganic materials 0.000 description 6
- 235000011152 sodium sulphate Nutrition 0.000 description 6
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L Calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 5
- 239000000292 calcium oxide Substances 0.000 description 4
- 235000019504 cigarettes Nutrition 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 229910052813 nitrogen oxide Inorganic materials 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- 239000004317 sodium nitrate Substances 0.000 description 4
- 235000010344 sodium nitrate Nutrition 0.000 description 4
- 229960003563 Calcium Carbonate Drugs 0.000 description 3
- 229910002089 NOx Inorganic materials 0.000 description 3
- 229910000019 calcium carbonate Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 239000012265 solid product Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 229960005069 Calcium Drugs 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000006011 modification reaction Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000005453 pelletization Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N Ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L Calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 210000003128 Head Anatomy 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 235000015450 Tilia cordata Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive Effects 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 235000011132 calcium sulphate Nutrition 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- -1 flue gas nitrogen oxides Chemical class 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000001939 inductive effect Effects 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000004301 light adaptation Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous Oxide Chemical class [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001105 regulatory Effects 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 239000001187 sodium carbonate Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 230000005619 thermoelectricity Effects 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
- B01D53/46—Removing components of defined structure
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
-
- 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
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/602—Oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The present invention provides flue gas and desulfurizing and denitrifying integrated purification system and purification method, the cleaning system includes desulfurization denitrification agent dosing system, recirculating fluidized bed, supply equipment is sprayed, gas-solid separation equipment and exhaust apparatus, desulfurization denitrification agent dosing system are connect with recirculating fluidized bed, the recirculating fluidized bed is passed through mouth equipped with flue gas, spray head is equipped in recirculating fluidized bed, the outlet side of recirculating fluidized bed is connect with gas-solid separation equipment, and the outlet side of gas-solid separation equipment is connect with exhaust apparatus.The cleaning system is carried out at the same time desulphurization denitration by same recirculating fluidized bed to flue gas, reduces flue gas desulfurization and denitrification cost；The purification method is directed to the characteristics of coal-fired flue-gas and low steel industry sintering flue gas temperature, desulphurization denitration is carried out at the same time to flue gas as desulfurization denitrification agent using calcium-base absorbing agent and sodium bicarbonate, flue gas after purified meets discharge relevant criterion, and by-product has certain economic benefit.
Description
Technical field
The invention belongs to filed of flue gas purification, are related to flue gas and desulfurizing and denitrifying integrated purification system and purification method,
More particularly to sintering flue gas and coal-fired flue-gas for steel industry.
Background technology
With economic development, the economy especially based on energy consumption increases rapidly, a large amount of plant emissions contain particulate matter,
SO2、NOX, the pollutants such as heavy metal flue gas, cause acid rain, haze and photochemical fog, people, animals and plants caused greatly to endanger
Evil.In order to meet the needs of people are for environmental protection, accelerate production of energy and consumption revolution process, industrial smoke discharges in country
Standard is gradually increased.2016《Steel sintering, pelletizing industrial air pollution object discharge standard》It is public discharge standard modification has been carried out
It accuses, the discharge limitation of sulfur dioxide, nitrogen oxides is adjusted again, it, should according to key area ambient air quality regulatory requirement
Further deepen steel sintering, the improvement of pelletizing industrial smoke, add tight especially emission limit requirement.About《Thermoelectricity atmosphere pollution
Discharge standard》(GB13223-2011) coal-burning boiler minimum discharge standard appearance, as coal unit minimum discharge limit value flue dust,
Sulfur dioxide, discharged nitrous oxides concentration (benchmark oxygen content 6%) are no more than 5mg/m respectively3、35mg/m3、50mg/m3.Therefore,
Control SO simultaneously2、NOxDischarge it is extremely urgent.
As the main source of industrial waste gas, coal-burning power plant of China used pollutant removing equipment instantly, due to going through
Most of history reason is that the function that different times are formed is single, the flue gas purifying equipment sequence that is used in series, and common is lime
The mode of stone-gypsum desulfurization+SCR denitration+electricity (bag) dedusting, due to domestic coal-fired from height ash, high-sulfur and fume treatment
Big present situation is measured, minimum discharge requirement can not be met using original technology.Steel and iron industry has obtained quick development in China, but
The pollution of its sintering flue gas but becomes a key factor for restricting China's metallurgy industry sustainable development.It is burnt caused by steel industry
Knot flue gas has the characteristics that exhaust temperature is relatively low, fluctuation range is big, water capacity is high, chemical constituent is complicated, particle diameter distribution is wide, mesh
Before, simple and effective comprehensive processing method is also lacked to flue gas and desulfurizing and denitrifying.Traditional administering method is in addition to in flue gas
Dust, SO2Outside being controlled, for NOxThe harmful substances such as, bioxin do not control effectively.Therefore, how dirty flue gas is carried out
Dye object overall-in-one control schema has become China environmental protection and realizes the inevitable choice of iron and steel metallurgical industry sustainable development.
At present, the main target as steel industry flue gas multiple pollutant overall-in-one control schema is to carry out desulfurization to sintering flue gas
Denitration, it is mainly combined with gas denitrifying technology by traditional desulfurization technology.In traditional desulfurization technology mostly using calcium base particle as
Desulfurizing agent has many advantages, such as that desulfurization effect is good (desulfuration efficiency up to more than 95%), stable, but also has floor space simultaneously
Greatly, operating cost is high, easily blocks, cannot effectively control NOxThe problems such as.Gas denitrifying technology mainly includes selective catalytic reduction
(SCR) and two kinds of non-selective catalytic reduction (SNCR).Temperature window needed for SNCR generally need to separately set and add up to 850-1050 DEG C
Thermal is by flue gas so far temperature window, and energy consumption is higher, and efficiency is low, therefore denitrating system is mostly based on SCR technology.
According to above-mentioned traditional desulfurization technology with the combined technique coordinated desulfurization denitration of gas denitrifying technology, though it can reach
The purpose of desulphurization denitration, but need the collaboration of more complete equipments, there are gross investment is big, complex process, take up a large area the problems such as.In addition,
Sintering flue gas has the characteristics of content of sulfur dioxide is high, temperature low (100-180 DEG C), according to SCR technology, one-time investment compared with
Height, the denitration efficiency of one layer of SCR catalyst then need two layers of SCR of arrangement only 50% or so to reach more than 75% denitration efficiency
Catalyst, but be difficult to meet the requirement that SCR catalyst reaction temperature is usually 300-450 DEG C, therefore need pair under this condition
Flue gas in denitrification process is heated.At the same time, using being also easy to produce ammonium sulfate and hydrogen sulfate in SCR technology denitrification process
Ammonium blocks SCR catalyst and SCR catalyst is poisoned, so that relevant cost increases.Therefore design research and development are a set of is suitable for
The technology of steel industry sintering flue gas and desulfurizing and denitrifying reduces the purified treatment cost of steel industry sintering flue gas, near pass
It is important.
Invention content
The present invention provides flue gas and desulfurizing and denitrifying integrated purifying system to overcome the problems in above-mentioned background technology
System, the cleaning system are carried out at the same time desulphurization denitration to flue gas by same recirculating fluidized bed, reduce flue gas desulfurization and denitrification cost；
The purification method is directed to the characteristics of coal-fired flue-gas and low steel industry sintering flue gas temperature, using calcium-base absorbing agent and sodium bicarbonate
Be carried out at the same time desulphurization denitration to flue gas as desulfurization denitrification agent, it is purified after flue gas meet discharge relevant criterion, by-product tool
There is certain economic benefit.
Flue gas and desulfurizing and denitrifying integrated purification system, including desulfurization denitrification agent dosing system, recirculating fluidized bed,
Supply equipment, gas-solid separation equipment and exhaust apparatus are sprayed, the denitration desulfurizing agent dosing system includes measurer, metering
Feeding device and dry powder playpipe, the discharge end of the measurer are connect with measuring the feed end of feeding device by pipeline, institute
The discharge end for stating metering feeding device is connect with the feed inlet of dry powder playpipe by pipeline, the jet port of the dry powder playpipe
It is connect with the feed inlet of recirculating fluidized bed, the recirculating fluidized bed is passed through mouth equipped with flue gas, and spray is equipped in recirculating fluidized bed
Head, the outlet side of the recirculating fluidized bed and the inlet end of gas-solid separation equipment are connected by pipeline, in the recirculating fluidized bed
Spray head with spray supply equipment connect by pipeline, the outlet side of gas-solid separation equipment is connect with exhaust apparatus.
Preferably, it is described metering feeding device claim including electron helical, rotary feeder, Pneumatic conveying pump, roots blower,
The feed end of the metering feeding device is the feed end that electron helical claims, and the discharge end that the electron helical claims is fed with rotation
The feed end connection of machine, the Pneumatic conveying pump include air inlet and accelerate mouth, dry-coal feeding mouth and accelerate dry powder discharge port, the rotation
The dry-coal feeding mouth of discharge end and Pneumatic conveying pump for turning batcher connects, the air outlet and Pneumatic conveying pump of the roots blower
Air inlet accelerate mouth connection, it is described metering feeding device discharge end be Pneumatic conveying pump acceleration dry powder discharge port.
Normally, the Pneumatic conveying pump is venturi loader, SK powders two-way valve or storehouse pump.
Normally, according to desulfurization denitrification agent straying quatity, multiple setting dry powder playpipes, multiple dry powder playpipes into
Material mouth is connected by the acceleration dry powder discharge port of lateral form and Pneumatic conveying pump.
Preferably, the spray supply equipment includes reservoir and water pump, and the water inlet end of water pump is connect with reservoir by pipeline,
Spray head in the water outlet and recirculating fluidized bed of water pump is connected by pipeline.The liquid in reservoir is supplied to by water pump and is followed
Spray head in ring fluid bed.
Preferably, the gas-solid separation equipment is sack cleaner.
Normally, the exhaust apparatus includes air-introduced machine and chimney, the outlet side of gas-solid separation equipment and air-introduced machine
Wind inlet end connected by pipeline, the outlet air end of air-introduced machine and the inlet end of chimney are connected by pipeline.
Preferably, the recirculating fluidized bed is continuous recirculating fluidized bed.
The continuous recirculating fluidized bed can be commercial equipment, and in order to reach better effect, the present invention provides continuous cycle
Fluid bed and intermittent cyclic fluid bed are as follows：
Preferably, the continuous recirculating fluidized bed includes flow reactor, cyclone dust collectors and back hopper, described continuous anti-
Answering device, flow reactor lower end is equipped with flue gas mixing-chamber for closed reactor, and flue gas mixing-chamber side is provided with flue gas and is passed through mouth,
Spray head is equipped in flow reactor above flue gas mixing-chamber, the top flow reactor side wall of spray head is equipped with the first charging
Mouthful, the first charging aperture is connect with the jet port of dry powder playpipe, and the flow reactor top is equipped with gas outlet, the outlet
Mouth is connect with the inlet end pipeline of cyclone dust collectors, and the cyclone dust collectors bottom end is equipped with ash bucket, the discharge end and feed back of ash bucket
The feed end connection of bucket, the discharge end of back hopper are connect with the second charging aperture that flow reactor side wall is set, and the whirlwind removes
The outlet side of dirt device is the outlet side of recirculating fluidized bed.
Preferably, the air inlet wind speed of the inlet end of cyclone dust collectors is at least 15m/s in the continuous recirculating fluidized bed.
Further, the flue gas mixing-chamber bottom end is equipped with waste pipe and corresponding mixing chamber waste valve.
Normally, the discharge end of the ash bucket is equipped with ash bucket discharge valve.Convenient for controlling the discharging speed of ash bucket so that its
In material can smoothly discharge.
Using the purification method of above-mentioned flue gas and desulfurizing and denitrifying integrated purification system, include the following steps：
(1) dispensing
Dispensing is carried out by following raw material proportioning：
30~100wt% of sodium bicarbonate powder
0~70wt% of dry powder class calcium-base absorbing agent
The good raw material of dispensing is uniformly mixed, obtains desulfurization denitrification agent；
(2) desulphurization denitration
Flue gas is passed through in recirculating fluidized bed, and passing through the penetrating atomized water of the spray head in recirculating fluidized bed increases flue gas
It is wet, while desulfurization denitrification agent is spurted into recirculating fluidized bed and is mixed with the flue gas after humidification, desulfurization denitrification agent passes through ciculation fluidized
It is purifying smoke by flue gas desulfurization and denitrification；Wherein, the amount for spurting into Na and Ca elemental substances in desulfurization denitrification agent adds up to：It is passed through cigarette
The amount of S and N element substance add up to=(1.2-2) in gas：1, in recirculating fluidized bed the Matter Transfer fluidisation time be at least 30min；
(3) gas solid separation, discharge
Purifying smoke after step (2) desulphurization denitration is subjected to gas solid separation processing, is then discharged.
Wherein, the grain size of desulfurization denitrification agent described in step (1) is not more than 75 μm.
Wherein, when being passed through SO in flue gas in step (2)2Content is 0~1000mg/m3, NO contents are 0~900mg/m3When,
The step (1) carries out dispensing by following raw material proportioning：
Sodium bicarbonate powder 100wt%
Dry powder class calcium-base absorbing agent 0wt%；
Or be,
SO in flue gas described in step (2)2Content is 1000~3500mg/m3, NO contents are 0~900mg/m3When,
The step (1) carries out dispensing by following raw material proportioning：
30~100wt% of sodium bicarbonate powder
0~70wt% of dry powder class calcium-base absorbing agent；
Normally, in desulfurization denitrification agent the proportion of dry powder class calcium-base absorbing agent with being passed through SO in flue gas2Content is improved and is increased
Add.
Wherein, water content is 10~20% in the flue gas in the step (2) after humidification.
Preferably, as the SO in flue gas described in step (2)2Content is 1800~2200mg/m3, NO contents for 700~
900mg/m3When, the step (1) carries out dispensing by following raw material proportioning：
55~50wt% of sodium bicarbonate powder
45~50wt% of dry powder class calcium-base absorbing agent；
Water content is 12~15% in flue gas in the step (2) after humidification.
Wherein, recirculating fluidized bed is continuous recirculating fluidized bed in the step (2), including flow reactor, cyclone dust removal
Device and back hopper, the flow reactor are closed reactor, and flow reactor lower end is equipped with flue gas mixing-chamber, flue gas mixing
Room side is provided with flue gas and is passed through mouth, and the spray head of atomized water, spray head are equipped in the flow reactor above flue gas mixing-chamber
Top flow reactor side wall be equipped with desulfurization denitrification agent penetrating first charging aperture, the flow reactor top is equipped with out
The inlet end pipeline connection of gas port, the gas outlet and cyclone dust collectors, the cyclone dust collectors bottom end are equipped with ash bucket, and ash bucket goes out
Expect that the feed end of end and back hopper connects, the discharge end of back hopper is connect with the second charging aperture that flow reactor side wall is set,
The outlet side of the cyclone dust collectors is the outlet side of recirculating fluidized bed, and the air inlet wind speed of the inlet end of cyclone dust collectors is at least
For 15m/s.
Normally, the dry powder class calcium-base absorbing agent is commercially available or is obtained with reference to prior art preparation, main component packet
Include calcium carbonate and calcium oxide one of which or two kinds.
Wherein, it is detached in recirculating fluidized bed is generated in the step (2) desulphurization denitration solid product and step (3)
The solid gone out, centralized recovery processing.
It is noted that it is detached in recirculating fluidized bed is generated in step (2) desulphurization denitration solid product and step (3)
The solid gone out, main component are the solid impurity in remaining unreacted desulfurization denitrification agent, sodium sulphate, sodium nitrate, flue gas, can
Sodium sulphate therein is isolated by the prior art it is used as the raw material of industry and uses or be the tools such as fertilizer by prior art preparation
The product having an economic benefit.
The principle of the present invention is as follows：
The main reaction formula of flue gas and desulfurizing and denitrifying integrated purifying method of the present invention is as follows：
4NaHCO3+2SO2+O2=2Na2CO3+4CO2+2H2O
4NaHCO3+2NO+O2=2NaNO3+2H2O+4CO2
2NaHCO3=Na2CO3+H2O+CO2
2NO+O2=2NO2
Na2CO3+3NO2=2NaNO3+NO+CO2
CaO+SO2=CaSO3
2CaSO3+O2=2CaSO4
CaO+H2O=Ca (OH)2
2Ca(OH)2+2SO2+O2=2CaSO4+2H2O
2CaCO3+2SO2+O2=2CaSO4+2CO2
Its cardinal principle for desulfurization denitrification agent after spraying into recirculating fluidized bed, mixed with the flue gas after humidification, utilize cigarette
Gas original temperature, desulfurization denitrification agent in reactor in flue gas nitrogen oxides, sulfur dioxide hybrid reaction, pass through complicated
Chemical reaction variation, by it is ciculation fluidized repeatedly after the product grain that generates due to agglomeration so that particle, which has to be granulated, imitates
Fruit exits cycle so as to deposit, achievees the purpose that while remove nitrogen oxides in effluent and sulfur dioxide.
Specifically, be that sodium bicarbonate in desulfurization denitrification agent is easily thermally decomposed to generate porous sodium carbonate, adsorb and with suction
Sulfur and nitrogen oxides generation sodium sulphate and the sodium nitrate in the flue gas after humidification are received, completes desulphurization denitration.Calcium base absorbs
Main component such as calcium carbonate (CaCO in agent3) or calcium oxide (CaO), under ciculation fluidized state low temperature is generated with water in humidification flue gas
Under highly active Ca (OH)2, Ca (OH)2With the SO in humidification flue gas2Gas liquid reaction occurs, is absorbed by chemically reacting
Oxysulfide, generation calcium sulfate (CaSO4) and then desulfurization.Under collective effect by calcium-base absorbing agent, sodium bicarbonate and water, make
Most of pollutant is removed in flue gas.
Present system can directly apply to the emission treatment of coal-fired flue-gas and sintering flue gas or directly be installed in combustion
The rear end of flue-gas processing equipment so that standard limit of smog release meets relevant regulations.
The invention has the advantages that：
1st, flue gas desulfurization, denitration and dedusting are carried out organic assembling and form a complete process system by present system,
The prior art that flue gas is independently carried out in desulphurization and denitration, dedusting links is simplified, so as to reduce up-front investment and running cost
With.
2nd, present system can be widely used in the smoke gas treatment of various kilns, including coal-burning boiler, sintering machine, cement
Kiln, coke oven etc., equipment is reliable, and service life is long, easy care, flue gas energy qualified discharge.
3rd, the present invention is mixed into additive with calcium-base absorbing agent and sodium bicarbonate and uses semidry-method recirculating fluidized bed technology,
120 DEG C of temperature or more can be reduced energy consumption, reduce operating cost directly using flue-gas temperature without reheating.
4th, for SO2A concentration of 3500mg/m3, a concentration of 900mg/m of NO3Place's purifying rate reaches more than 95%, efficiently
Remove the SO in flue gas2、NOXWait sour gas.
5th, by-product of the invention can be used as in industry and agricultural for calcium sulfate, sodium sulphate and sodium nitrate etc. and recycle profit
With avoiding secondary pollution and bring economic benefits simultaneously.
Description of the drawings
Fig. 1 is a kind of structure diagram of flue gas and desulfurizing and denitrifying integrated purification system of the present invention.
In figure, 1 measurer, 1-1 dispensing valves, 2 electron helicals claim, 3 rotary feeders, 4 roots blowers, 5 Pneumatic conveying pumps,
6 dry powder playpipes, 6-1 dry powder injection valves, 7 gas-solid separation equipments, 8 air-introduced machines, 9 chimneys, 10 flow reactors, 10-1 cigarettes
Gas mixing chamber, 10-2 mixing chamber waste valves, 11 cyclone dust collectors, 11-1 ash bucket discharge valves, 12 back hoppers, 21 flue gas access tubes,
22 reservoirs, 23 water pumps, 24 spray heads.
Specific embodiment
The invention will be further described by way of example and in conjunction with the accompanying drawings.It is worth noting that the implementation provided
Example is it is not intended that limiting the scope of the invention, person skilled in art's content according to the present invention make the present invention
Some the nonessential modifications and adaptations gone out should belong to the scope of the present invention.
As shown in Figure 1, the present embodiment provides flue gas and desulfurizing and denitrifying integrated purification system, including desulfurization denitrification agent
Dosing system, continuous recirculating fluidized bed spray supply equipment, gas-solid separation equipment 7 and exhaust apparatus, the denitration desulfurization
Agent dosing system includes measurer 1, metering feeding device and dry powder playpipe 6, and the metering feeding device includes electronics
Spiral claims 2, rotary feeder 3, Pneumatic conveying pump 5, roots blower 4, and the Pneumatic conveying pump 5 is venturi loader, including
Air inlet accelerates mouth, dry-coal feeding mouth and accelerates dry powder discharge port, and the continuous recirculating fluidized bed includes flow reactor 10, whirlwind
Deduster 11 and back hopper 12, the spray supply equipment include reservoir 22 and water pump 23, and the exhaust apparatus includes air-introduced machine 8
With chimney 9；
The discharge end of the measurer 1 claims 2 feed end to be connect by pipeline with electron helical, and passes through dispensing valve 1-1
It is controlled, the electron helical claims 2 discharge end to be connect with the feed end of rotary feeder 3, the discharge end of rotary feeder 3
Connect with the dry-coal feeding mouth of Pneumatic conveying pump 5 by pipeline, the air outlet of the roots blower 4 and Pneumatic conveying pump 5 into
Wind accelerates mouth to be connected by pipeline, and the acceleration dry powder discharge port and the feed inlet of dry powder playpipe 6 of the Pneumatic conveying pump 5 pass through
Pipeline connects, and passes through dry powder injection valve 6-1 and controlled, in the jet port of the dry powder playpipe 6 and flow reactor 10
Portion connects；
The flow reactor 10 is closed reactor, and flue gas mixing-chamber 10-1 is equipped in 10 lower end of flow reactor,
It is connected with flue gas access tube 21 on flue gas mixing-chamber 10-1 side walls, flue gas mixing-chamber 10-1 bottom ends are equipped with waste pipe and right therewith
Spray head 24 is equipped in the flow reactor above mixing chamber waste valve 10-2, flue gas mixing-chamber 10-1 answered, spray head 24
Top flow reactor side wall is equipped with first charging aperture, and the first charging aperture is connect with the jet port of dry powder playpipe 6, described
The outlet side that flow reactor 10 is located at top is connect with the inlet end of cyclone dust collectors 11 by pipeline, the cyclone dust collectors
11 lower ends are equipped with ash bucket, and the discharge end of ash bucket is connect with the feed end of back hopper 12, and is passed through ash bucket discharge valve 11-1 and controlled
System, the discharge end of the back hopper 12 are connect with the second charging aperture that 10 side wall of flow reactor is set；Cyclone dust collectors 11
The air inlet wind speed of inlet end is at least 15m/s；
The water inlet end of the water pump 23 is connect with reservoir 22 by pipeline, the water outlet of water pump 23 and continuous recirculating fluidized bed
Interior spray head 24 is connected by pipeline；
The outlet side of the cyclone dust collectors 11 is connect with the inlet end of gas-solid separation equipment 7 by pipeline, the gas-solid
Separation equipment 7 is sack cleaner, and the outlet side of gas-solid separation equipment 7 is connect with the wind inlet end of air-introduced machine 8 by pipeline, air inducing
The outlet air end of machine 8 is connect with the inlet end of chimney 9 by pipeline, and the flue gas after desulphurization denitration is arranged by chimney
It puts.
Using the purification method of above-mentioned flue gas and desulfurizing and denitrifying integrated purification system, include the following steps：
(1) dispensing
Dispensing is carried out according to embodiment ratio each in table 1, the good raw material of dispensing is uniformly mixed, obtains desulfurization denitrification agent；
(2) desulphurization denitration
Flue gas is passed through in continuous recirculating fluidized bed, and pass through the penetrating atomized water of the spray head in continuous recirculating fluidized bed to make
Flue gas is humidified, while desulfurization denitrification agent is spurted into recirculating fluidized bed and is mixed with the flue gas after humidification, and desulfurization denitrification agent is by following
Flue gas desulfurization and denitrification is purifying smoke by circulation；Wherein, SO in each embodiment flue gas2Content, NO contents, flue gas flow, cigarette
For temperature degree with reference to table 1, the amount of Na and Ca elemental substances in desulfurization denitrification agent of spurting into adds up to and is passed through S and N element object in flue gas
The amount of matter the ratio between adds up to reference to each embodiment in table 1, and the flue gas water content after humidification is with reference to each embodiment in table 1；
(3) gas solid separation, discharge
Purifying smoke after step (2) desulphurization denitration is subjected to gas solid separation processing, is then discharged.
Table 1
The grain size of the desulfurization denitrification agent is not more than 75 μm.
Normally, the dry powder class calcium-base absorbing agent is commercially available or is obtained with reference to prior art preparation, main component packet
Include calcium carbonate and calcium oxide one of which or two kinds.
Wherein, it is detached in recirculating fluidized bed is generated in the step (2) desulphurization denitration solid product and step (3)
The solid gone out, centralized recovery processing, main component is in remaining unreacted desulfurization denitrification agent, sodium sulphate, sodium nitrate, flue gas
Solid impurity, sodium sulphate therein can be isolated by the prior art is used as the raw material of industry and use or pass through the prior art
Being prepared as fertilizer etc. has the product of economic benefit.
Claims (10)
1. flue gas and desulfurizing and denitrifying integrated purification system, it is characterised in that including desulfurization denitrification agent dosing system, follow
Ring fluid bed sprays supply equipment, gas-solid separation equipment (7) and exhaust apparatus, the denitration desulfurizing agent dosing system packet
Include measurer (1), metering feeding device and dry powder playpipe (6), discharge end and the metering feeding device of the measurer (1)
Feed end is connected by pipeline, and the feed inlet of the discharge end and dry powder playpipe (6) of the metering feeding device is connected by pipeline
It connects, the jet port of the dry powder playpipe (6) and the feed inlet of recirculating fluidized bed connect, and the recirculating fluidized bed is equipped with flue gas
Be passed through mouth, be equipped with spray head (24) in recirculating fluidized bed, the outlet side of the recirculating fluidized bed and gas-solid separation equipment (7) into
Gas end is connected by pipeline, and the spray head (24) in the recirculating fluidized bed is connect with spray supply equipment by pipeline, gas-solid
The outlet side of separation equipment (7) is connect with exhaust apparatus.
2. flue gas and desulfurizing and denitrifying integrated purification system according to claim 1, it is characterised in that it is described measure to
Material equipment claims (2), rotary feeder (3), Pneumatic conveying pump (5), roots blower (4), the metering feed including electron helical
The feed end of equipment claims the feed end of (2) for electron helical, and the electron helical claims the discharge end of (2) and rotary feeder (3)
Feed end connection, the Pneumatic conveying pump (5) include air inlet accelerate mouth, dry-coal feeding mouth and accelerate dry powder discharge port, it is described
The discharge end of rotary feeder (3) is connect with the dry-coal feeding mouth of Pneumatic conveying pump (5), the air outlet of the roots blower (4)
Mouth is accelerated to connect with the air inlet of Pneumatic conveying pump (5), the discharge end of the metering feeding device is the acceleration of Pneumatic conveying pump (5)
Dry powder discharge port.
3. flue gas and desulfurizing and denitrifying integrated purification system according to claim 1 or 2, it is characterised in that the strength
Delivery pump (5) is venturi loader, SK powders two-way valve or storehouse pump；The gas-solid separation equipment (7) is sack cleaner；Institute
It states exhaust apparatus and includes air-introduced machine (8) and chimney (9), the outlet side of gas-solid separation equipment (7) and the inlet air of air-introduced machine (8)
End is connected by pipeline, and the outlet air end of air-introduced machine (8) and the inlet end of chimney are connected by pipeline.
4. flue gas and desulfurizing and denitrifying integrated purification system according to claim 1 or 2, it is characterised in that the cycle
Fluid bed be continuous recirculating fluidized bed, the continuous recirculating fluidized bed include flow reactor (10), cyclone dust collectors (11) and
Back hopper (12), the flow reactor (10) are closed reactor, and flow reactor (10) lower end is equipped with flue gas mixing-chamber
(10-1), flue gas mixing-chamber (10-1) side are provided with flue gas and are passed through mouth, in the flow reactor above flue gas mixing-chamber (10-1)
Equipped with spray head (24), the top flow reactor side wall of spray head (24) is equipped with first charging aperture, the first charging aperture with
The jet port connection of dry powder playpipe (6), flow reactor (10) top is equipped with gas outlet, the gas outlet and cyclone dust removal
The inlet end pipeline connection of device (11), cyclone dust collectors (11) bottom end is equipped with ash bucket, the discharge end and back hopper of ash bucket
(12) feed end connection, the discharge end of back hopper (12) is connect with the second charging aperture that flow reactor side wall is set, described
The outlet side of cyclone dust collectors (11) is the outlet side of recirculating fluidized bed.
5. flue gas and desulfurizing and denitrifying integrated purification system according to claim 4, it is characterised in that the spray supplies
Wetting system includes reservoir (22) and water pump (23), and the water inlet end of water pump (23) is connect with reservoir (22) by pipeline, water pump (23)
Water outlet and recirculating fluidized bed in spray head (24) connected by pipeline.
6. flue gas and desulfurizing and denitrifying integrated purification system according to claim 4, it is characterised in that the flue gas mixes
It closes room (10-1) bottom end and is equipped with waste pipe and corresponding mixing chamber waste valve (10-2).
7. using any flue gas and desulfurizing and denitrifying integrated purification systems of claim 1-6 purification method, including with
Lower step：
(1) dispensing
Dispensing is carried out by following raw material proportioning：
30~100wt% of sodium bicarbonate powder
0~70wt% of dry powder class calcium-base absorbing agent
The good raw material of dispensing is uniformly mixed, obtains desulfurization denitrification agent；
(2) desulphurization denitration
Flue gas is passed through in recirculating fluidized bed, and passing through the penetrating atomized water of the spray head in recirculating fluidized bed makes flue gas be humidified, together
When by desulfurization denitrification agent spurt into recirculating fluidized bed with humidification after flue gas mix, desulfurization denitrification agent is by ciculation fluidized by flue gas
Desulphurization denitration is purifying smoke；Wherein, the amount for spurting into Na and Ca elemental substances in desulfurization denitrification agent adds up to：It is passed through S in flue gas
Add up to=(1.2-2) with the amount of N element substance：1, in recirculating fluidized bed the Matter Transfer fluidisation time be at least 30min；
(3) gas solid separation, discharge
Purifying smoke after step (2) desulphurization denitration is subjected to gas solid separation processing, is then discharged.
8. purification method according to claim 7, it is characterised in that when being passed through SO in flue gas in step (2)2Content for 0~
1000mg/m3, NO contents are 0~900mg/m3When, the step (1) carries out dispensing by following raw material proportioning：
Sodium bicarbonate powder 100wt%
Dry powder class calcium-base absorbing agent 0wt%；
Or be,
SO in flue gas described in step (2)2Content is 1000~3500mg/m3, NO contents are 0~900mg/m3When, it is described
Step (1) carries out dispensing by following raw material proportioning：
30~100wt% of sodium bicarbonate powder
0~70wt% of dry powder class calcium-base absorbing agent.
9. purification method according to claim 7, it is characterised in that water content is in the flue gas in the step (2) after humidification
10~20%.
10. purification method according to claim 7, it is characterised in that recirculating fluidized bed is continuous cycle in the step (2)
Fluid bed, including flow reactor, cyclone dust collectors and back hopper, the flow reactor is closed reactor, continuous anti-
Device lower end is answered to be equipped with flue gas mixing-chamber, flue gas mixing-chamber side is provided with flue gas and is passed through mouth, the successive reaction above flue gas mixing-chamber
The spray head of atomized water is equipped in device, the top flow reactor side wall of spray head is equipped with the first of desulfurization denitrification agent penetrating
Feed inlet, the flow reactor top are equipped with gas outlet, and the inlet end pipeline connection of the gas outlet and cyclone dust collectors is described
Cyclone dust collectors bottom end is equipped with ash bucket, and the feed end of the discharge end of ash bucket and back hopper connects, the discharge end of back hopper with it is continuous
The second charging aperture connection of sidewall of reactor setting, the outlet side of the cyclone dust collectors are the outlet side of recirculating fluidized bed, and
The air inlet wind speed of the inlet end of cyclone dust collectors is at least 15m/s.
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| CN113144862A (en) * | 2020-12-24 | 2021-07-23 | 上海康恒环境股份有限公司 | Biomass incineration power generation flue gas ultralow emission system and emission method thereof |
| CN113144772A (en) * | 2021-04-30 | 2021-07-23 | 青铜峡铝业股份有限公司宁东铝业分公司 | Two-section type electrolytic flue gas purification and discharge device, control system and method |
| CN113144772B (en) * | 2021-04-30 | 2022-10-14 | 青铜峡铝业股份有限公司宁东铝业分公司 | Two-section type electrolytic flue gas purification and discharge device, control system and method |
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