CN107890771A - A kind of flue gas low-temperature dry desulfurization denitration process system and method - Google Patents
A kind of flue gas low-temperature dry desulfurization denitration process system and method Download PDFInfo
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- CN107890771A CN107890771A CN201711143695.9A CN201711143695A CN107890771A CN 107890771 A CN107890771 A CN 107890771A CN 201711143695 A CN201711143695 A CN 201711143695A CN 107890771 A CN107890771 A CN 107890771A
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 99
- 230000023556 desulfurization Effects 0.000 title claims abstract description 99
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 65
- 239000003546 flue gas Substances 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 60
- 230000008569 process Effects 0.000 title claims abstract description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 33
- 239000000779 smoke Substances 0.000 claims abstract description 32
- 230000003321 amplification Effects 0.000 claims abstract description 29
- 238000003199 nucleic acid amplification method Methods 0.000 claims abstract description 29
- 238000009692 water atomization Methods 0.000 claims abstract description 11
- 239000004744 fabric Substances 0.000 claims abstract description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 44
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 21
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 10
- 239000005864 Sulphur Substances 0.000 claims description 9
- 239000000428 dust Substances 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 6
- 238000013461 design Methods 0.000 claims description 5
- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 230000005540 biological transmission Effects 0.000 claims description 3
- 239000010959 steel Substances 0.000 claims description 3
- 240000007594 Oryza sativa Species 0.000 claims description 2
- 235000007164 Oryza sativa Nutrition 0.000 claims description 2
- 235000009566 rice Nutrition 0.000 claims description 2
- 238000003672 processing method Methods 0.000 abstract 1
- 238000010586 diagram Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 235000019504 cigarettes Nutrition 0.000 description 3
- 238000005187 foaming Methods 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 235000010891 Ptelea trifoliata Nutrition 0.000 description 1
- 244000097592 Ptelea trifoliata Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000010410 dusting Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000000007 visual effect 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
- B01D53/346—Controlling the process
-
- 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
- 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
-
- 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
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of flue gas low-temperature dry desulfurization denitration process system and processing method, including inlet sensor group, reactor, water pump, air-introduced machine, water pump, PLC and data acquisition unit, the smoke inlet end is provided with inlet sensor group, and the end at smoke inlet end is fixed with flashboard air deflector, the smoke inlet end is connected with volume amplification region, water atomizing nozzle is provided with the volume amplification region, and the end of volume amplification region is connected with reaction zone, reactor sensor group is provided with the reaction zone, and feed bin is fixed with reaction zone, the both sides of the feed bin are fixed with screen cloth, the outside of the screen cloth is provided with drenching sprayer, the water atomizing nozzle and drenching sprayer are connected with water pump, the end of the reaction zone is fixedly connected with smoke outlet, air-introduced machine is fixed with the smoke outlet.The system has that technological process is short, equipment is simple, fault rate is low, easy to maintain, employment is few, takes up an area and space very little, operating cost are low.
Description
Technical field
At flue gas desulfurization and denitrification systems technology field, more particularly to a kind of flue gas low-temperature dry desulfurization denitration
Manage system and method.
Background technology
It can produce substantial amounts of pollution flue gas with the quickening of process of industrialization, in industrial production, caused sulfur-bearing in flue gas,
Nitrogen-containing oxide (NOX), dust and moisture are discharged with flue gas, cause environmental pollution, and the processing for pollutant in flue gas accounts for work
Larger ratio in industry production cost.However, lime stone --- the gypsum+selective-catalytic-reduction denitrified that traditional handicraft uses
(SCR) technique is big due to investing, it is difficult to be received by enterprise.Investment is big, operating cost is high, again can not without newly-increased economic benefit
The bottlenecks such as desulfurization (SO2) denitration (NOX) simultaneously annoying always has become various countries using enterprise, desulfurization and denitrification integral process
Control the research and development focus of smoke pollution.
The content of the invention
It is contemplated that at least solves one of technical problem in correlation technique to a certain extent.Therefore, the present invention
One purpose is to propose a kind of flue gas low-temperature dry desulfurization denitration process system and method, and investment, technique can be greatly decreased
Flow is short, equipment is simple, fault rate is low, easy to maintain, employment is few, takes up an area and space very little, and operating cost is low, no secondary wastewater
And dust emission, construction period significantly shorten.
The technical scheme is that：
A kind of flue gas low-temperature dry desulfurization denitration process system, including inlet sensor group, reactor, water pump, air-introduced machine,
Water pump, PLC and data acquisition unit, the middle part top of the reactor are fixed with crane runway, the company of slip on the crane runway
Crane hoisting machine is connected to, the material that the shell of reactor uses is steel, and the reactor includes smoke inlet end, volume is amplified
Area, reaction zone and smoke outlet, the smoke inlet end is provided with inlet sensor group, and the end at smoke inlet end is fixed with
Flashboard air deflector, the gate valve of the flashboard air deflector electrically connect with PLC, and the smoke inlet end is connected with volume amplification region,
Water atomizing nozzle is provided with the volume amplification region, and the end of volume amplification region is connected with reaction zone, in the reaction zone
Provided with reactor sensor group, and feed bin is fixed with reaction zone, the both sides of the feed bin are fixed with screen cloth, the screen cloth it is outer
Side is provided with drenching sprayer, and the water atomizing nozzle and drenching sprayer are connected with water pump, and the water pump electrically connects with PLC, institute
The end for stating reaction zone is fixedly connected with smoke outlet, is fixed with air-introduced machine in the smoke outlet, the air-introduced machine with
PLC is electrically connected.
Preferably, the inlet sensor group includes temperature sensor, flow sensor and dust sensor, and data are equal
Transmit to PLC.
Preferably, the reactor sensor group includes charging aperture sensor group and intermediate layer sensor group, the charging
Before mouthful sensor group is arranged on the first layer of reaction zone, and charging aperture sensor group includes air velocity transducer, temperature sensor, wet
Spend sensor and sulphur/amount of nitrogen oxides sensor；
The intermediate layer sensor group is arranged on reaction zone intermediate layer and discharge outlet, and intermediate layer sensor group includes
Humidity sensor and sulphur/amount of nitrogen oxides sensor, the charging aperture sensor group and intermediate layer sensor group data pass
PLC is transported to, the PLC electrically connects with data acquisition unit, and the data acquisition unit is by network to server transmission data.
Preferably, deflector is provided with the reactor, the deflector is connected with the port of export of flashboard air deflector.
The desulfurization denitration method of above-mentioned flue gas low-temperature dry desulfurization denitration process system, is to be handled as follows：
1), according to the operating mode of desulphurization denitration, desulfurization denitrification agent and reactor design are configured so that body of the flue gas in reactor
Volume is enlarged into 15-40 times of former flue cross section product by product amplification region；
2) several air channels, are formed by flashboard air deflector water conservancy diversion in the volume amplification region of reactor；
3), by the charge basket equipped with desulfurization denitrification agent according to transverse horizontal air intake, the vertical desulfurization denitrification agent section of reaching
Mode is fixed in each air channel in feed bin, if dried layer desulfurization denitrification agent is placed in each air channel；
4), the flue gas after dedusting is passed through in reactor, controls the flow velocity of smoke inlet so that flue gas reaches after water conservancy diversion
The flow velocity in out of stock dose of section of first layer desulfurization is less than 5m/s；
5), by the water atomizing nozzle of volume amplification region to flue gas cool-down so that flue-gas temperature is carried out at 45-350 DEG C
Reaction, while sprayed water using drenching sprayer to desulfurization denitrification agent.
Preferably, the consumption of desulfurization denitrification agent is in the step 1)：When carrying out desulfurization process, desulfurization amount takes off with desulfurization
The ratio of nitre agent is 1:(1-1.2)；When carrying out denitration process, the ratio of denitration amount and desulfurization denitrification agent is 10:1.
Preferably, the number in the step 2) air channel is 2-12.
Preferably, 2-10 layers are placed in out of stock dose of desulfurization in reactor in the step 3), and gross thickness is 2.0-10.0 rice.
Preferably, preferable reaction temperature is 45-80 DEG C in the step 5).
Preferably, the mass ratio of desulfurization denitrification agent and water is 1 in the step 5):(1.1-1.4).
Beneficial effects of the present invention：The system of the present invention is desulphurization denitration at low temperatures, passes through flashboard air deflector pair
The flue gas of arrival end is shunted, and makes the flow velocity in each air channel consistent；Can be to flue gas by the atomizing water nozzle of volume amplification region
Cool and reduce gas flow rate, while alarm function is may also function as under overrun condition；Pass through arrival end sensor group and reaction
The data such as flow, humidity, temperature and the content of device sensor group monitoring flue gas；Flue gas can be monitored by reactor sensor group to exist
The related data of reaction zone；Blower fan, water pump, valve and the operation of other executing agencies is controlled to complete fume treatment by PLC
Production；Data acquisition unit can be easy to that technical specialist's is long-range by the data collected by network transmission to server or high in the clouds
Analysis, diagnose without being in the action, improve the operating efficiency of high-level technical staff.
Compared with conventional wet, the system investment is greatly decreased, and technological process is short, equipment is simple, fault rate is low, is easy to
Maintenance, employment are few, and occupation of land and space very little, operating cost is low, and no secondary wastewater and dust emission, the construction period significantly shorten.
Brief description of the drawings
Accompanying drawing is used for providing a further understanding of the present invention, and a part for constitution instruction, the reality with the present invention
Apply example to be used to explain the present invention together, be not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is a kind of process flow diagram of flue gas low-temperature dry desulfurization denitration process system proposed by the present invention；
Fig. 2 is a kind of process system block diagram of flue gas low-temperature dry desulfurization denitration process system proposed by the present invention；
Fig. 3 is the vertical view of reactor in a kind of flue gas low-temperature dry desulfurization denitration process system and method proposed by the present invention
Schematic diagram；
Fig. 4 is the side view of reactor in a kind of flue gas low-temperature dry desulfurization denitration process system and method proposed by the present invention
Schematic diagram.
In figure：1- flashboards air deflector, 2- feed bins, 3- screen clothes, 4- drenching sprayers, 5- deflectors, 6- air-introduced machines, 7- crane rails
Road, 8- crane hoisting machines.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear, complete
Site preparation describes, it is clear that described embodiment is only part of the embodiment of the present invention, rather than whole embodiments.
The example of the embodiment is shown in the drawings, wherein same or similar label represents identical or class from beginning to end
As element or with same or like function element.The embodiments described below with reference to the accompanying drawings are exemplary, purport
For explaining the present invention, and it is not considered as limiting the invention.
In the description of the invention, it is to be understood that term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", " on ", " under ", "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom " " interior ", " outer ", " up time
The orientation or position relationship of the instruction such as pin ", " counterclockwise ", " axial direction ", " radial direction ", " circumference " be based on orientation shown in the drawings or
Position relationship, it is for only for ease of and describes the present invention and simplify description, rather than indicates or imply that signified device or element must
There must be specific orientation, with specific azimuth configuration and operation, therefore be not considered as limiting the invention.
In addition, term " first ", " second " are only used for describing purpose, and it is not intended that instruction or hint relative importance
Or the implicit quantity for indicating indicated technical characteristic.Thus, define " first ", the feature of " second " can be expressed or
Implicitly include one or more this feature.In the description of the invention, " multiple " are meant that two or more,
Unless otherwise specifically defined.
In the present invention, unless otherwise clearly defined and limited, term " installation ", " connected ", " collection ", " upload ",
The term such as " delivering to ", " control ", " connection ", " fixation " should be interpreted broadly, for example, it may be being fixedly connected or can
Dismantling connection, or integrally；Can be mechanical connection or electrical connection；Can be joined directly together, centre can also be passed through
Medium is indirectly connected, and can be connection or the interaction relationship of two elements of two element internals.For the general of this area
For logical technical staff, the concrete meaning of above-mentioned term in the present invention can be understood as the case may be.
Embodiment 1
Reference picture 3-4, a kind of flue gas low-temperature dry desulfurization denitration process system, including inlet sensor group, reactor, water
Pump, air-introduced machine 6, water pump, PLC and data acquisition unit, the material that the shell of reactor uses is steel, and the middle part of reactor is pushed up
End is fixed with crane runway 7, crane hoisting machine 8 is slidably connected on the crane runway 7, the reactor includes smoke inlet
End, volume amplification region, reaction zone and smoke outlet, the smoke inlet end are provided with inlet sensor group, and smoke inlet end
End be fixed with flashboard air deflector 1, using six flashboard mixing air deflectors in the present embodiment, the flashboard air deflector 1
Gate valve is controlled by PLC, and the smoke inlet end is connected with volume amplification region, and atomized water is provided with the volume amplification region and is sprayed
Head, and the end of volume amplification region is connected with reaction zone, and reactor sensor group is provided with the reaction zone, and in reaction zone
Feed bin 2 is fixed with, the both sides of the feed bin 2 are fixed with screen cloth 3, and the outside of the screen cloth 3 is provided with drenching sprayer 4, the atomization
Sprinkler head and drenching sprayer 4 are connected with water pump, and the water pump is controlled by PLC, the end of the reaction zone and exhanst gas outlet
End is fixedly connected, and air-introduced machine 6 is fixed with the smoke outlet, and air-introduced machine 6 is controlled by PLC.
The inlet sensor group includes temperature sensor, flow sensor and dust sensor, and is connected with PLC.
The reactor sensor group includes charging aperture sensor group and intermediate layer sensor group, the charging aperture sensor
Before group is arranged on the first layer of reaction zone, and charging aperture sensor group includes temperature sensor, humidity sensor and sulphur/nitrogen oxidation
Thing content level sensor, the intermediate layer sensor group are arranged on reaction zone intermediate layer and discharge outlet, and intermediate layer sensor
Group includes humidity sensor and sulphur/amount of nitrogen oxides sensor, and the charging aperture sensor group and intermediate layer sensor group are equal
It is connected with PLC, the data acquisition unit is connected with PLC.
Deflector 5 is provided with the reactor, the deflector 5 is connected with the port of export of flashboard air deflector 1.
Selected by reactor it is temperature/flow/wind speed/pressure integral sensor in embodiment, model：VF210；
The model of sulphur/NOx sensor：KM905；The model of humidity sensor：SHT series；The model of dust sensor
For：PM2010；PLC model S300；Data acquisition unit model XD8000.
Desulphurization denitration processing is carried out using the desulfurization denitrification agent of independent development in reference picture 1-2, embodiment 2-4, is matched somebody with somebody
Fang Wei：1 part of metal carbonate, 9 parts of metal oxide, 2 parts of metal sulfate, 1 part of magnesium chloride, 0.3 part of silica, oxidation are sub-
0.5 part of iron, 0.5 part of aluminum oxide.By water ash weight than 1:2 weigh raw material, and input stirring foaming machine stirring tune homogeneous paste is simultaneously defeated
Deliver to and 60min is aerated in aerator, volume is increased to 1.3 times；Raw material after above-mentioned aeration is continued in foaming machine is stirred
Stirring foaming 30min, produces porous expander, volume is increased to 5.5 times, divides natural drying solidification；Treat porous expander
Split after solidification；Desulfurization denitrification agent is placed and adds up to 180 tons in reactor.
Embodiment 2
A kind of desulfurization denitration method of flue gas low-temperature dry desulfurization denitration process system, is to be handled as follows：
1), according to the operating mode of desulphurization denitration, desulfurization denitrification agent is configured, the consumption metering of wherein desulfurization denitrification agent is as follows：
During desulfurization process, the ratio of desulfurization amount and desulfurization denitrification agent is 1:1；When carrying out denitration process, denitration amount and desulfurization denitrification agent
Ratio is 10:1；
According to desulphurization denitration amount reactor design so that volume is enlarged into former cigarette by flue gas in the volume amplification region of reactor
30 times of road sectional area；
2) 6 air channels, are formed by flashboard air deflector water conservancy diversion in the volume amplification region of reactor；
3), by the charge basket equipped with desulfurization denitrification agent according to transverse horizontal air intake, the vertical desulfurization denitrification agent section of reaching
Mode is fixed in each air channel in feed bin, and each air channel places 2 layers, and gross thickness is 2.0 meters；
4), the flue gas after dedusting is passed through in reactor, controls the flow velocity of smoke inlet so that flue gas reaches after water conservancy diversion
The flow velocity in out of stock dose of section of first layer desulfurization is less than 5m/s；
5), by the water atomizing nozzle of volume amplification region to flue gas cool-down so that flue-gas temperature is reacted at 45 DEG C,
Sprayed water simultaneously using drenching sprayer to desulfurization denitrification agent, the mass ratio of desulfurization denitrification agent and water is 1:1.1.
Embodiment 3
A kind of desulfurization denitration method of flue gas low-temperature dry desulfurization denitration process system, is to be handled as follows：
1), according to the operating mode of desulphurization denitration, desulfurization denitrification agent is configured, the consumption metering of wherein desulfurization denitrification agent is as follows：
During desulfurization process, the ratio of desulfurization amount and desulfurization denitrification agent is 1:1.2；When carrying out denitration process, denitration amount and desulfurization denitrification agent
Ratio be 10:1；
According to desulphurization denitration amount reactor design so that volume is enlarged into former cigarette by flue gas in the volume amplification region of reactor
18 times of road sectional area；
2) 12 air channels, are formed by flashboard air deflector water conservancy diversion in the volume amplification region of reactor；
3), by the charge basket equipped with desulfurization denitrification agent according to transverse horizontal air intake, the vertical desulfurization denitrification agent section of reaching
Mode is fixed in each air channel in feed bin, and each air channel places 6 layers, and gross thickness is 3.6 meters；
4), the flue gas after dedusting is passed through in reactor, controls the flow velocity of smoke inlet so that flue gas reaches after water conservancy diversion
The flow velocity in out of stock dose of section of first layer desulfurization is less than 5m/s；
5), by the water atomizing nozzle of volume amplification region to flue gas cool-down so that flue-gas temperature is reacted at 80 DEG C,
Sprayed water simultaneously using drenching sprayer to desulfurization denitrification agent, the mass ratio of desulfurization denitrification agent and water is 1:1.25.
Embodiment 4
A kind of desulfurization denitration method of flue gas low-temperature dry desulfurization denitration process system, is to be handled as follows：
1), according to the operating mode of desulphurization denitration, desulfurization denitrification agent is configured, the consumption metering of wherein desulfurization denitrification agent is as follows：
During desulfurization process, the ratio of desulfurization amount and desulfurization denitrification agent is 1:1.1；When carrying out denitration process, denitration amount and desulfurization denitrification agent
Ratio be 10:1；
According to desulphurization denitration amount reactor design so that volume is enlarged into former cigarette by flue gas in the volume amplification region of reactor
35 times of road sectional area；
2) 3 air channels, are formed by flashboard air deflector water conservancy diversion in the volume amplification region of reactor；
3), by the charge basket equipped with desulfurization denitrification agent according to transverse horizontal air intake, the vertical desulfurization denitrification agent section of reaching
Mode is fixed in each air channel in feed bin, and each air channel places 8 layers, and gross thickness is 6 meters；
4), the flue gas after dedusting is passed through in reactor, controls the flow velocity of smoke inlet so that flue gas reaches after water conservancy diversion
The flow velocity in out of stock dose of section of first layer desulfurization is less than 5m/s；
5), by the water atomizing nozzle of volume amplification region to flue gas cool-down so that flue-gas temperature is carried out instead at 300 DEG C
Should, while sprayed water using drenching sprayer to desulfurization denitrification agent, the mass ratio of desulfurization denitrification agent and water is 1:1.4.
Embodiment or workflow：In use, first by after flue gas rough dusting so that desulphurization denitration material is placed on
In feed bin 2, flue gas enters from smoke inlet end, and temperature, flow and the dust content of flue gas are can detect by inlet sensor group,
Shunted by flashboard air deflector 1 and imported into by deflector 5 in different air channels, pass through the atomizing water nozzle of volume amplification region
After flue gas cool-down, it is passed into reaction zone, temperature, the humidity of reaction zone flue gas is entered by the detection of charging aperture sensor group
And the data such as sulphur/amount of nitrogen oxides, and reaction zone intermediate layer and discharge outlet flue gas are detected by intermediate layer sensor group
The data such as humidity and sulphur/amount of nitrogen oxides, it is visual by computer etc. after gathering by data acquisition unit and upload to high in the clouds
Change interface to carry out remotely monitoring, scheduling process data and combine software mathematical model and manual analysis, formulate rational production system
Spend, and the operation of blower fan, water pump, valve is controlled by PLC, realize automated production.
In the present invention, unless otherwise clearly defined and limited, fisrt feature can be with "above" or "below" second feature
It is that the first and second features directly contact, or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature are directly over second feature or oblique upper, or be merely representative of
Fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " can be
One feature is immediately below second feature or obliquely downward, or is merely representative of fisrt feature level height and is less than second feature.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means specific features, structure, material or the spy for combining the embodiment or example description
Point is contained at least one embodiment or example of the present invention.In this manual, to the schematic representation of above-mentioned term not
Necessarily refer to identical embodiment or example.Moreover, specific features, structure, material or the feature of description can be any
One or more embodiments or example in combine in an appropriate manner.
The foregoing is only a preferred embodiment of the present invention, but protection scope of the present invention be not limited thereto,
Any one skilled in the art the invention discloses technical scope in, technique according to the invention scheme and its
Inventive concept is subject to equivalent substitution or change, should all be included within the scope of the present invention.
Claims (10)
1. a kind of flue gas low-temperature dry desulfurization denitration process system, including inlet sensor group, reactor, water pump, air-introduced machine, water
Pump, PLC and data acquisition unit, the middle part top of the reactor are fixed with crane runway, are slidably connected on the crane runway
There is crane hoisting machine, it is characterised in that：The material that the shell of reactor uses is steel, and the reactor includes smoke inlet
End, volume amplification region, reaction zone and smoke outlet, the smoke inlet end are provided with inlet sensor group, and smoke inlet end
End be fixed with flashboard air deflector, the gate valve of the flashboard air deflector is electrically connected with PLC, and the smoke inlet end is put with volume
Great Qu is connected, and water atomizing nozzle is provided with the volume amplification region, and the end of volume amplification region is connected with reaction zone, institute
State and reactor sensor group is provided with reaction zone, and feed bin is fixed with reaction zone, the both sides of the feed bin are fixed with screen cloth, institute
The outside for stating screen cloth is provided with drenching sprayer, and the water atomizing nozzle and drenching sprayer are connected with water pump, the water pump and PLC
Electrical connection, the end of the reaction zone are fixedly connected with smoke outlet, and air-introduced machine is fixed with the smoke outlet, described
Air-introduced machine electrically connects with PLC.
2. flue gas low-temperature dry desulfurization denitration process system according to claim 1, it is characterised in that：The entrance sensing
Device group includes temperature sensor, flow sensor and dust sensor, and data are transmitted to PLC.
3. flue gas low-temperature dry desulfurization denitration process system according to claim 1, it is characterised in that：The reactor passes
Sensor group includes charging aperture sensor group and intermediate layer sensor group, and the charging aperture sensor group is arranged on the first of reaction zone
Before layer, and charging aperture sensor group includes air velocity transducer, temperature sensor, humidity sensor and sulphur/amount of nitrogen oxides and passed
Sensor；
The intermediate layer sensor group is arranged on reaction zone intermediate layer and discharge outlet, and intermediate layer sensor group includes humidity
Sensor and sulphur/amount of nitrogen oxides sensor, the charging aperture sensor group and intermediate layer sensor group data transmit to
PLC, the PLC electrically connect with data acquisition unit, and the data acquisition unit is by network to server transmission data.
4. flue gas low-temperature dry desulfurization denitration process system according to claim 1, it is characterised in that：In the reactor
Provided with deflector, the deflector is connected with the port of export of flashboard air deflector.
5. the desulfurization denitration method of flue gas low-temperature dry desulfurization denitration process system according to claim 1, its feature exist
In：Handled as follows：
1), according to the operating mode of desulphurization denitration, desulfurization denitrification agent and reactor design are configured so that flue gas is put in the volume of reactor
Volume is enlarged into 15-40 times of former flue cross section product by great Qu；
2) several air channels, are formed by flashboard air deflector water conservancy diversion in the volume amplification region of reactor；
3), by the charge basket equipped with desulfurization denitrification agent in the way of transverse horizontal air intake, vertical arrival desulfurization denitrification agent section
It is fixed in each air channel in feed bin, if dried layer desulfurization denitrification agent is placed in each air channel；
4), the flue gas after dedusting is passed through in reactor, controls the flow velocity of smoke inlet so that flue gas reaches first after water conservancy diversion
The flow velocity in out of stock dose of section of layer desulfurization is less than 5m/s；
5), by the water atomizing nozzle of volume amplification region to flue gas cool-down so that flue-gas temperature is reacted at 45-350 DEG C,
Sprayed water simultaneously using drenching sprayer to desulfurization denitrification agent.
6. the desulfurization denitration method of flue gas low-temperature dry desulfurization denitration process system according to claim 5, its feature exist
In：The consumption of desulfurization denitrification agent is in the step 1)：When carrying out desulfurization process, the ratio of desulfurization amount and desulfurization denitrification agent is
1:(1-1.2)；When carrying out denitration process, the ratio of denitration amount and desulfurization denitrification agent is 10:1.
7. the desulfurization denitration method of flue gas low-temperature dry desulfurization denitration process system according to claim 5, its feature exist
In：The number in the step 2) air channel is 2-12.
8. the desulfurization denitration method of flue gas low-temperature dry desulfurization denitration process system according to claim 5, its feature exist
In：2-10 layers are placed in out of stock dose of desulfurization in reactor in the step 3), and gross thickness is 2.0-10.0 rice.
9. the desulfurization denitration method of flue gas low-temperature dry desulfurization denitration process system according to claim 5, its feature exist
In：Preferable reaction temperature is 45-80 DEG C in the step 5).
10. the desulfurization denitration method of flue gas low-temperature dry desulfurization denitration process system according to claim 5, its feature exist
In：The mass ratio of desulfurization denitrification agent and water is 1 in the step 5):(1.1-1.4).
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| CN201711143695.9A CN107890771A (en) | 2017-11-17 | 2017-11-17 | A kind of flue gas low-temperature dry desulfurization denitration process system and method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112657315A (en) * | 2019-10-15 | 2021-04-16 | 中国石油化工股份有限公司 | Method and system for treating epichlorohydrin waste gas |
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| JPH10272340A (en) * | 1997-03-31 | 1998-10-13 | Nippon Steel Corp | Denitration process for coke oven exhaust gas |
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