CN108465371A - One kind being based on minimum discharge fume treatment running gear and processing method - Google Patents
One kind being based on minimum discharge fume treatment running gear and processing method Download PDFInfo
- Publication number
- CN108465371A CN108465371A CN201810527231.6A CN201810527231A CN108465371A CN 108465371 A CN108465371 A CN 108465371A CN 201810527231 A CN201810527231 A CN 201810527231A CN 108465371 A CN108465371 A CN 108465371A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- flue
- heat
- depickling
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000003672 processing method Methods 0.000 title claims abstract description 10
- 239000003517 fume Substances 0.000 title claims abstract description 8
- 239000003546 flue gas Substances 0.000 claims abstract description 119
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 90
- 238000000034 method Methods 0.000 claims abstract description 60
- 238000010531 catalytic reduction reaction Methods 0.000 claims abstract description 32
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 24
- 230000008569 process Effects 0.000 claims description 16
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 15
- 239000000908 ammonium hydroxide Substances 0.000 claims description 15
- 229910021529 ammonia Inorganic materials 0.000 claims description 12
- 238000010790 dilution Methods 0.000 claims description 11
- 239000012895 dilution Substances 0.000 claims description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 claims description 7
- 239000000779 smoke Substances 0.000 claims description 7
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 6
- 230000008901 benefit Effects 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 230000009467 reduction Effects 0.000 claims description 6
- 238000006722 reduction reaction Methods 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 6
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 5
- 230000003197 catalytic effect Effects 0.000 claims description 5
- 238000006555 catalytic reaction Methods 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 239000004744 fabric Substances 0.000 claims description 4
- 239000000243 solution Substances 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 239000006227 byproduct Substances 0.000 claims description 3
- 239000003054 catalyst Substances 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 3
- 229910052602 gypsum Inorganic materials 0.000 claims description 3
- 239000010440 gypsum Substances 0.000 claims description 3
- 238000007689 inspection Methods 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 230000008439 repair process Effects 0.000 claims description 3
- 239000011780 sodium chloride Substances 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 230000001360 synchronised effect Effects 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 claims description 2
- 230000009286 beneficial effect Effects 0.000 claims 1
- 230000005611 electricity Effects 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 8
- 238000001035 drying Methods 0.000 abstract description 5
- 239000010813 municipal solid waste Substances 0.000 abstract description 4
- 235000019504 cigarettes Nutrition 0.000 description 4
- 239000002253 acid Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- WWILHZQYNPQALT-UHFFFAOYSA-N 2-methyl-2-morpholin-4-ylpropanal Chemical compound O=CC(C)(C)N1CCOCC1 WWILHZQYNPQALT-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 230000009466 transformation 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
- B01D53/74—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
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
- B01D46/023—Pockets filters, i.e. multiple bag filters mounted on a common frame
-
- 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
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- 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
- 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
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention relates to one kind being based on minimum discharge fume treatment running gear and processing method, suitable for city garbage burning power plant, it discloses using traditional non-selective catalytic reduction denitration technology+semidry method/dry-process deacidification+bag filter and increases the device and processing method of wet method depickling+low-temperature selective catalytic reduction fume treatment, the range of operation of unit load can be not only widened in this way, and can also meet the needs of flue gas minimum discharge.
Description
Technical field
The present invention relates to the fume treatment fields of garbage incinerating power plant, in particular for the minimum discharge of flue gas.
Background technology
Minimizing, recycling, innoxious may be implemented using the method for burning disposal in rubbish, but in Refuse Incineration Process
It will produce the pernicious gases such as HCL, SO2, NOx.Burning power plant would generally use non-selective catalytic reduction denitration technology+
" semidry method/dry-process deacidification+bag filter " handles flue gas, but NOx emission can be caused exceeded when unit is in heavy-duty service,
At this time in order to meet the requirement of flue gas qualified discharge, it has to reduce unit load, influence economic benefit.Simultaneously using non-selection
Property catalytic-reduction denitrified technology needs ammonia is sprayed in stove, excessive ammonia can cause the escaping of ammonia, and react generation with the SO3 in flue gas
NH4HSO4 blocks bag filter, reduces the removal efficiency to dust.In addition to this, semidry method/dry-process deacidification technique is by flue gas
Temperature is affected, and deacidification efficiency is low compared to wet method depickling, cannot be guaranteed that flue gas is up to standard when load is higher.
Invention content
The object of the present invention is to provide based on minimum discharge fume treatment running gear and method, it is in bag filter
Wet method depickling+low-temperature selective catalytic reduction denitration is added below, makes to run under unit high load capacity, improves generated energy, Er Qieke
To meet the requirement of flue gas minimum discharge.
The technology of the present invention solution is in incinerator, non-selective catalytic reduction denitration, half-dried reaction tower, bag-type dust
Device, bag filter outlet, feature are that flue gas enters flue gas-flue gas heat-exchange unit one by bag filter outlet, enter back into wet method
The wet scrubber tower of depickling processing, after the wet scrubber tower, into the packing channel in flue gas-flue gas heat-exchange unit two after it is straight
It taps into and chimney is introduced by air-introduced machine into the flue in steam-flue gas heat-exchange unit, then chosen property catalytic reduction reactor, from selection
Property catalytic reduction reactor flue in synchronized splitter part of smoke through heat dilution wind turbine, after electric heater, evaporated into ammonium hydroxide
Mixing module after carrying out heating dilution to ammonium hydroxide, sprays into " ∩ types " flue, in scr reactor by ammonia-spraying grid
The interior NOx with flue gas reacts, then is sent to smokestack by air-introduced machine and be discharged into air.
It is non-selection that the minimum discharge flue gas processing method of the present invention is that flue gas that incinerator goes out conventionally first carries out
Property catalytic-reduction denitrified processing, pass through half-reaction tower and carry out semidry method depickling processing, after bag filter is handled, in flue gas
Still contain exceeded flue gas content NOx, SOx, feature of the present invention is to increase wet method depickling+low temperature on conventional process flow tail portion
Selective catalytic reduction flue gas treatment process.Flue gas enters one lower layer part of flue gas-flue gas heat-exchange unit from bag filter outlet, so
Tower is washed by wet type and carries out wet method depickling processing, further the sour gas of 90% or more removal, the cigarette of wet scrubber tower outlet
About 60~70 DEG C of temperature degree, then passes through the high temperature cigarette of one upper layer part of flue gas-flue gas heat-exchange unit and wet scrubber tower entrance again
After gas heat exchange, so that flue-gas temperature is increased to about 125 DEG C, then pass through flue gas-flue gas heat-exchange unit two and selective catalytic reduction again
The high-temperature flue gas of reactor outlet exchanges heat, and flue gas is made further to be promoted, by the flue gas after flue gas-flue gas heat-exchange unit two again by
Steam-flue gas heat-exchange unit further heats up, and flue gas is entered scr reactor, chosen property to 170 DEG C
After catalytic reduction reactor, flue gas divides primary and secondary two tunnels, and main flue gas road sprays into chimney through air-introduced machine, and secondary gas flue is through heat dilution wind
Machine carries out heating dilution after electric heater into ammonium hydroxide evaporator mixing module to ammonium hydroxide, when to be mixed into design dense for ammonium hydroxide evaporation
When spending, then flue is sprayed by ammonia-spraying grid and is sufficiently mixed with flue gas, flue gas enters scr reactor inlet temperature
Promotion, other than carrying out steam-flue gas heat-exchange unit, some come from selective catalysis reduction reactor outlet high temperature
Flue gas improves utilization rate of waste heat.Under the catalytic action of low-temperature selective catalytic reduction reactor, it can be gone through decomposing NOx
Except 90% or more NOx, flue gas reaches minimum discharge standard.
For the cleaning solution that the wet method depickling of the above present invention uses for NaOH, the primary product NaCl of generation is dissolved in water, avoids
The by-product gypsum generated using limewash depickling, causes line clogging, meanwhile, scr reactor 10 is arranged in
Behind deacidification system, dust content in flue gas, SO2 and other harmful substances are considerably less at this time, non-to the denitration efficiency of catalyst
Chang Youli.
When the semidry method or wet method unit ad hoc inspection and repair of the present invention, arbitrary a set of unit can be used and adjust operating parameter to cigarette
Gas carries out efficient depickling, ensures that flue gas emission is up to standard, in addition to this, is optimized and revised by what is utilized to two-stage unit, Neng Goushi
Meet the purpose of flue gas qualified discharge under present optimum economic benefit.
The present invention can be subtracted by optimizing non-selective catalytic reduction and the selective catalytic reduction combined denitration method of operation
The dosage of small ammonia prevents the escaping of ammonia and the generation of NH4HSO4, avoids strong cohesive property of the cloth bag due to NH4HSO4, results in blockage.
Using non-selective catalytic reduction denitration technology+semidry method/dry-process deacidification+bag filter+wet method depickling+low
Temperature selective catalytic reducing smoke treatment technology increases wet method depickling+cryogenic selective catalysis also in original technological process
Former denitration process technique can not only widen the range of operation of unit load, and can also meet flue gas minimum discharge in this way
Demand.
Compared with prior art, the present invention has the following advantages：
(1) requirement that disclosure satisfy that unit heavy-duty service flue gas qualified discharge, improves economic benefit.
(2) when joint is using low-temperature selective catalytic reduction denitration, it is avoided that being sprayed at non-selective catalytic reduction denitration
Enter excessive ammonia, cause the escaping of ammonia, ammonium hydrogen sulfate is caused to block the generation of cloth bag phenomenon.
(3) semidry method/dry-process deacidification is 85% to the removal efficiency of SO2, and wet method depickling reaches the removal efficiency of SO2
To 95%, sour gas can further be removed, meet the requirement of minimum discharge.
(4) flue gas-flue gas heat-exchange unit is installed, the heat of tail portion high-temperature flue gas is made full use of to heat low-temperature flue gas, reduces
The input of external heat source.
Description of the drawings
Fig. 1 is traditional type flue gas treating process flow diagram；
Fig. 2 is flue gas treating process flow diagram of the present invention.
Specific implementation mode
Implementation steps are as follows：
(1) the flue gas treating process flow before Fig. 1 is transformation.The technological process includes：Incinerator 13 non-selective is urged
Change reduction denitration 14, half-dried reaction tower 15, bag filter 16, bag filter outlet 1, chimney.Rubbish is in incinerator 13
It burns the flue gas generated and first passes around the progress denitration process of non-selective catalytic reduction device 14, next passes through half-dried reaction tower
15 carry out semidry method depickling processing, then flow through 16 dedusting of bag filter, are finally discharged into air by chimney.This fume treatment
Technique is in unit heavy-duty service, it is difficult to meet the requirement of minimum discharge.
(2) Fig. 2 is flue gas treating process of the present invention, and technological process is to be added to wet method on the basis of original technique to take off
Acid and low-temperature selective catalytic reduction denitration treatment technology.The technique includes：Flue gas enters flue gas-cigarette by bag filter outlet 1
Gas heat exchanger 1, the wet scrubber tower 3 for reentering wet method depickling processing change after the wet scrubber tower 3 into flue gas-flue gas
Flue in straight steam-flue gas heat-exchange unit 8 after packing channel in hot device 27, then chosen property catalytic reduction reactor 10
Chimney is introduced by air-introduced machine 11, synchronized splitter part of smoke is through heat dilution wind from scr reactor flue 10
Machine 4 after electric heater 5, evaporates mixing module 6 into ammonium hydroxide, after carrying out heating dilution to ammonium hydroxide, is sprayed by ammonia-spraying grid 9
" ∩ types " flue is reacted with the NOx in flue gas in the scr reactor 10, then by air-introduced machine 11 send to
Smokestack 12 is discharged into air.
(3) minimum discharge flue gas processing method of the present invention is that flue gas enters wet scrubber tower 3 from bag filter outlet 1
Depickling processing is carried out, treated, and flue gas flows through one upper layer part 2 of flue gas-flue gas heat-exchange unit, and flue gas-flue gas heat-exchange unit 27 steams
Vapour-flue gas heat-exchange unit 8 carries out flue gas, and after reaching assigned temperature, denitration is carried out into scr reactor 10
Processing, treated, and clean flue gas is discharged into air through air-introduced machine by chimney.
(4) flue gas can remove 80% or more sour gas after semidry method depickling processing, using the wet of back segment
Formula scrubbing tower 3 carries out wet method depickling processing, and can further remove 90% or more sour gas so that flue gas meets ultralow row
The requirement put.
(5) flue-gas temperature that wet scrubber tower 3 exports is about 60~70 DEG C, passes through one upper layer of flue gas-flue gas heat-exchange unit
Portion 2 makes flue-gas temperature be increased to about 125 DEG C, then passes through cigarette again with after the high-temperature flue gas heat exchange of 3 entrance of wet scrubber tower
The high-temperature flue gas that gas-flue gas heat-exchange unit 27 is exported with scr reactor 10 exchanges heat, and keeps smoke temperature further
It is promoted.
(6) flue gas after the heat absorption of flue gas-flue gas heat-exchange unit 27, then further heated up and (adopted by steam-flue gas heat-exchange unit 8
Heated with 4.0 megapascal superheated steams), by flue gas to 170 DEG C of entrance scr reactors 10.
(7) part of smoke is extracted out from 10 flue of scr reactor through heat dilution wind turbine 4, electric heater
After 5, heating dilution is carried out to ammonium hydroxide into ammonium hydroxide evaporation mixing module 6, when ammonium hydroxide evaporation is mixed into design concentration, then by spraying
Ammonia grid 9 sprays into flue, is sufficiently mixed with flue gas, under the catalytic action of low-temperature selective catalytic reduction reactor 10, decomposes
NOx。
(8) NOx in flue gas is after early period non-selective catalytic reduction denitration process in incinerator, 60% or so in flue gas
NOx can effectively remove, after the chosen property catalytic reduction reactor of remaining NOx 10, and can further remove 90% or more
NOx can make the NOx in flue gas meet the requirement of minimum discharge using combined purifying denitrating flue gas treatment process.
(9) promotion of 10 entrance flue gas temperature of scr reactor, in addition to coming from steam-flue gas heat-exchange unit
Outside 8, some comes from the high-temperature flue gas of the outlet of scr reactor 10, substantially increases in this way more than flue gas
The efficiency of heat utilization improves the economy of power plant.
(10) for the cleaning solution that the depickling of this technique wet method uses for NaOH, the primary product NaCl of generation is dissolved in water, avoids adopting
The by-product gypsum generated with limewash depickling, causes line clogging.Meanwhile scr reactor 10 be arranged in it is de-
Behind acid system, dust content in flue gas, SO2 and other harmful substances are considerably less at this time, very to the denitration efficiency of catalyst
Favorably.
(11) semidry method or when wet method unit ad hoc inspection and repair, can be used arbitrary a set of unit adjustment operating parameter to flue gas into
The efficient depickling of row ensures that flue gas emission is up to standard.In addition to this, it is optimized and revised, can be realized by what is utilized to two-stage unit
Meet the purpose of flue gas qualified discharge under optimum economic benefit.
(12) by optimizing non-selective catalytic reduction and the selective catalytic reduction combined denitration method of operation, can reduce
The dosage of ammonia prevents the escaping of ammonia and the generation of NH4HSO4, avoids strong cohesive property of the cloth bag due to NH4HSO4, results in blockage.
Claims (5)
1. one kind being based on minimum discharge fume treatment running gear, including incinerator, non-selective catalytic reduction denitration is half-dried anti-
Tower, bag filter, bag filter outlet, chimney are answered, it is characterized in that flue gas enters flue gas-flue gas by bag filter outlet
Heat exchanger one enters back into the wet scrubber tower of wet method depickling processing, after the wet scrubber tower, into flue gas-flue gas heat exchange
Be directly entered after packing channel in device two flue in steam-flue gas heat-exchange unit, then chosen property catalytic reduction reactor by
Air-introduced machine introduces chimney, and synchronized splitter part of smoke is through heat dilution wind turbine, electricity from scr reactor flue
After heater, mixing module is evaporated into ammonium hydroxide, after carrying out heating dilution to ammonium hydroxide, " ∩ types " flue is sprayed by ammonia-spraying grid,
It reacts with the NOx in flue gas in scr reactor, then is sent to smokestack by air-introduced machine and be discharged into air.
2. one kind is based on minimum discharge flue gas processing method, including the flue gas that goes out of incinerator conventionally first carry out it is non-selection
Property catalytic-reduction denitrified processing, pass through half-reaction tower and carry out semidry method depickling processing, after bag filter is handled, in flue gas
Still contain exceeded flue gas content NOx, SOx, the present invention it is characterized in that, increase wet method depickling+low on conventional process flow tail portion
Temperature selective catalytic reducing smoke treatment process, flue gas enter one lower layer part of flue gas-flue gas heat-exchange unit from bag filter outlet,
Then wet method depickling processing is carried out through wet scrubber tower, further the sour gas of 90% or more removal, wet scrubber tower outlet
About 60~70 DEG C of flue-gas temperature, then pass through the height of flue gas-flue gas heat-exchange unit one upper layer part and wet scrubber tower entrance again
After warm flue gas heat exchange, so that flue-gas temperature is increased to about 125 DEG C, then pass through flue gas-flue gas heat-exchange unit two and selective catalysis again
The high-temperature flue gas of reduction reactor outlet exchanges heat, and so that flue gas is further promoted, by the flue gas after flue gas-flue gas heat-exchange unit two
It is further heated up again by steam-flue gas heat-exchange unit, flue gas is entered into scr reactor to 170 DEG C, through choosing
After selecting property catalytic reduction reactor, flue gas divides primary and secondary two tunnels, and main flue gas road sprays into chimney through air-introduced machine, and secondary gas flue is dilute through heat
It releases wind turbine, heating dilution is carried out to ammonium hydroxide into ammonium hydroxide evaporator mixing module after electric heater, set when ammonium hydroxide evaporation is mixed into
When counting concentration, then flue is sprayed by ammonia-spraying grid and is sufficiently mixed with flue gas, flue gas enters scr reactor entrance
The promotion of temperature, other than carrying out steam-flue gas heat-exchange unit, some comes from the outlet of selective catalysis reduction reactor
High-temperature flue gas improves utilization rate of waste heat.Under the catalytic action of low-temperature selective catalytic reduction reactor, through decomposing NOx
90% or more NOx can be removed, flue gas reaches minimum discharge standard.
3. according to claim 2 processing method, it is characterized in that：The cleaning solution that wet method depickling uses is NaOH, the main production of generation
Object NaCl is dissolved in water, avoids the by-product gypsum generated using limewash depickling, causes line clogging, meanwhile, selective catalysis
Reduction reactor 10 is arranged in behind deacidification system, and dust content in flue gas, SO2 and other harmful substances are considerably less at this time, right
The denitration efficiency of catalyst is highly beneficial.
4. according to claim 2 processing method, it is characterized in that：When the semidry method or wet method unit ad hoc inspection and repair of the present invention, it can adopt
Efficient depickling is carried out to flue gas with arbitrary a set of unit adjustment operating parameter, ensures that flue gas emission is up to standard, in addition to this, by right
What two-stage unit utilized optimizes and revises, and can realize the purpose for meeting flue gas qualified discharge under optimum economic benefit.
5. according to claim 2 processing method, it is characterized in that：The present invention is urged by optimizing non-selective catalytic reduction and selectivity
Change reduction the combined denitration method of operation, the dosage of ammonia can be reduced, prevent the escaping of ammonia and the generation of NH4HSO4, avoid cloth bag by
In the strong cohesive property of NH4HSO4, result in blockage.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810527231.6A CN108465371A (en) | 2018-05-29 | 2018-05-29 | One kind being based on minimum discharge fume treatment running gear and processing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810527231.6A CN108465371A (en) | 2018-05-29 | 2018-05-29 | One kind being based on minimum discharge fume treatment running gear and processing method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108465371A true CN108465371A (en) | 2018-08-31 |
Family
ID=63261493
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810527231.6A Pending CN108465371A (en) | 2018-05-29 | 2018-05-29 | One kind being based on minimum discharge fume treatment running gear and processing method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108465371A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109092039A (en) * | 2018-10-11 | 2018-12-28 | 广州环投设计研究院有限公司 | A kind of flexible and efficient ultra-clean fume treatment technology |
| CN109925869A (en) * | 2019-04-12 | 2019-06-25 | 洁华控股股份有限公司 | Flue gas of refuse burning high-efficient purification processing method |
| CN110433654A (en) * | 2019-08-08 | 2019-11-12 | 光大环保能源(杭州)有限公司 | A kind of smoke gas comprehensive treatment system |
| CN111346509A (en) * | 2020-04-28 | 2020-06-30 | 苏州西热节能环保技术有限公司 | Diagnosis method for ammonium bisulfate poisoning of SCR denitration catalyst |
| WO2023236318A1 (en) * | 2022-06-06 | 2023-12-14 | 深圳华明环保科技有限公司 | Flue gas treatment process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN206652386U (en) * | 2016-12-31 | 2017-11-21 | 上海康恒环境股份有限公司 | A kind of minimum discharge purifier of burning city domestic garbage flue gas |
| CN208526306U (en) * | 2018-05-29 | 2019-02-22 | 广州环投设计研究院有限公司 | One kind being based on minimum discharge fume treatment running gear |
-
2018
- 2018-05-29 CN CN201810527231.6A patent/CN108465371A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN206652386U (en) * | 2016-12-31 | 2017-11-21 | 上海康恒环境股份有限公司 | A kind of minimum discharge purifier of burning city domestic garbage flue gas |
| CN208526306U (en) * | 2018-05-29 | 2019-02-22 | 广州环投设计研究院有限公司 | One kind being based on minimum discharge fume treatment running gear |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109092039A (en) * | 2018-10-11 | 2018-12-28 | 广州环投设计研究院有限公司 | A kind of flexible and efficient ultra-clean fume treatment technology |
| CN109925869A (en) * | 2019-04-12 | 2019-06-25 | 洁华控股股份有限公司 | Flue gas of refuse burning high-efficient purification processing method |
| CN110433654A (en) * | 2019-08-08 | 2019-11-12 | 光大环保能源(杭州)有限公司 | A kind of smoke gas comprehensive treatment system |
| CN111346509A (en) * | 2020-04-28 | 2020-06-30 | 苏州西热节能环保技术有限公司 | Diagnosis method for ammonium bisulfate poisoning of SCR denitration catalyst |
| WO2023236318A1 (en) * | 2022-06-06 | 2023-12-14 | 深圳华明环保科技有限公司 | Flue gas treatment process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN206652386U (en) | A kind of minimum discharge purifier of burning city domestic garbage flue gas | |
| CN108465371A (en) | One kind being based on minimum discharge fume treatment running gear and processing method | |
| CN108636098A (en) | A kind of the minimum discharge purifier and its method of burning city domestic garbage flue gas | |
| CN110624384A (en) | Purification treatment method and purification treatment device for waste incineration flue gas | |
| CN105289248B (en) | Wet-type purification treatment method and device for flue gas of household garbage incineration power plant | |
| CN112121614A (en) | Stable ultralow emission device and method for solid waste incineration flue gas | |
| CN101907406A (en) | Flue gas utilization and treatment system for industrial stoves | |
| CN210699488U (en) | Full-green clean production process equipment for glass kiln | |
| CN106492621A (en) | A kind of incinerator two-part flue gas purification system | |
| CN109482049A (en) | A kind of coke oven flue gas dry desulfurization denitration purification integral process | |
| CN113776061A (en) | Hazardous waste incineration flue gas purification and waste heat recovery device and method thereof | |
| CN212188526U (en) | Flue gas treatment system after sludge treatment | |
| CN217016043U (en) | Flue gas treatment system | |
| CN104329946B (en) | A kind of coke oven flue exhaust gas denitration and the integral system of waste heat recovery | |
| CN103691267A (en) | Low-temperature synchronous denitration and desulfurization equipment and process for flue gas | |
| CN208809774U (en) | A kind of ultra-clean purification system of flue gas | |
| CN106178877A (en) | A kind of coke oven flue waste gas purification waste heat recovery apparatus and technique | |
| CN102309920A (en) | Method for removing NOx and SOx from fluid catalytic cracking (FCC) flue gas | |
| CN211502852U (en) | Smoke tower integrated waste incineration smoke purification treatment device | |
| CN206535421U (en) | A kind of waste incinerator two-part flue gas purification system | |
| CN211585963U (en) | Purification treatment device for waste incineration flue gas | |
| CN208526306U (en) | One kind being based on minimum discharge fume treatment running gear | |
| CN211435768U (en) | Flue gas treatment device for semi-dry desulfurization and low-temperature SCR denitration of carbide slag | |
| CN112546832A (en) | Advanced treatment system and treatment method for waste incineration flue gas | |
| CN201764834U (en) | Utilization and treatment device for industrial kiln fume |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180831 |