CN114797441A - Clinker production device - Google Patents
Clinker production device Download PDFInfo
- Publication number
- CN114797441A CN114797441A CN202210509986.XA CN202210509986A CN114797441A CN 114797441 A CN114797441 A CN 114797441A CN 202210509986 A CN202210509986 A CN 202210509986A CN 114797441 A CN114797441 A CN 114797441A
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- CN
- China
- Prior art keywords
- flue gas
- spray head
- clinker production
- purifying agent
- smoke exhaust
- 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.)
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 34
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 93
- 239000003546 flue gas Substances 0.000 claims abstract description 93
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 71
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 64
- 239000000779 smoke Substances 0.000 claims abstract description 50
- 239000012629 purifying agent Substances 0.000 claims abstract description 44
- 238000005507 spraying Methods 0.000 claims abstract description 36
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 claims abstract description 28
- 230000007246 mechanism Effects 0.000 claims abstract description 10
- 239000007921 spray Substances 0.000 claims description 38
- 239000007788 liquid Substances 0.000 claims description 31
- 239000000463 material Substances 0.000 claims description 29
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 16
- 238000003860 storage Methods 0.000 claims description 15
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- 239000007789 gas Substances 0.000 claims description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 8
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 8
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 8
- 230000009471 action Effects 0.000 claims description 7
- 239000000428 dust Substances 0.000 claims description 7
- 239000011248 coating agent Substances 0.000 claims description 5
- 238000000576 coating method Methods 0.000 claims description 5
- ZKQDCIXGCQPQNV-UHFFFAOYSA-N Calcium hypochlorite Chemical compound [Ca+2].Cl[O-].Cl[O-] ZKQDCIXGCQPQNV-UHFFFAOYSA-N 0.000 claims description 4
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 claims description 4
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 4
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 4
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 4
- 239000000292 calcium oxide Substances 0.000 claims description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 4
- 239000012295 chemical reaction liquid Substances 0.000 claims description 4
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 claims description 4
- 239000001095 magnesium carbonate Substances 0.000 claims description 4
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims description 4
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 4
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 4
- 238000001802 infusion Methods 0.000 claims description 2
- 238000006477 desulfuration reaction Methods 0.000 abstract description 13
- 230000023556 desulfurization Effects 0.000 abstract description 13
- 235000010269 sulphur dioxide Nutrition 0.000 description 28
- 238000005245 sintering Methods 0.000 description 22
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical group [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 18
- 238000000034 method Methods 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 12
- 239000003344 environmental pollutant Substances 0.000 description 11
- 231100000719 pollutant Toxicity 0.000 description 11
- 230000008569 process Effects 0.000 description 10
- 230000008859 change Effects 0.000 description 9
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 9
- 235000017557 sodium bicarbonate Nutrition 0.000 description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- 239000012459 cleaning agent Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 229910001868 water Inorganic materials 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 230000000630 rising effect Effects 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 238000006479 redox reaction Methods 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000003929 acidic solution Substances 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000013067 intermediate product Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 241000482268 Zea mays subsp. mays Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000004291 sulphur dioxide Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000007723 transport mechanism Effects 0.000 description 1
Images
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
- B01D53/81—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
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
-
- 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
- B01D53/508—Sulfur oxides by treating the gases with solids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
- B01D53/565—Nitrogen oxides by treating the gases with solids
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/106—Peroxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/108—Halogens or halogen compounds
-
- 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
- B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
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- 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
- B01D2251/604—Hydroxides
-
- 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
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- 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
Abstract
The invention discloses a clinker production device, which comprises: the conveying mechanism is used for conveying the clinker; the smoke exhaust pipeline is arranged below the conveying mechanism and used for exhausting smoke generated by the clinker; and the spraying device is used for spraying a purifying agent to the flue gas in the flue gas exhaust pipeline, and the purifying agent is used for reacting with any one or more of sulfur dioxide, sulfur trioxide and nitrogen oxide in the flue gas. According to the clinker production device, the spraying device is arranged, the purifying agent can be sprayed to the flue gas in the flue gas exhaust pipeline through the spraying device, and the purifying agent can react with any one or more of sulfur dioxide, sulfur trioxide and nitrogen oxide in the flue gas, so that the flue gas is subjected to desulfurization and denitrification.
Description
Technical Field
The invention relates to the technical field of clinker production equipment, in particular to a clinker production device.
Background
In the steel smelting process, the treatment and purification of the sintering flue gas of industrial waste gas with the largest quantity, more concentrated pollutant types and higher concentration in the sintering process is the key point of energy conservation and emission reduction of atmospheric pollutants in the metallurgical industry. The desulfurization and the denitration are carried out separately in the process of the sintering flue gas treatment at the present stage, and the occupied area is huge. In China, tail end pollution treatment processes such as an SCR method and the like are commonly adopted for denitration of sintering machines. Because the sintering flue gas can not reach the catalytic reaction temperature of the SCR, the sintering flue gas needs to be heated for the second time, and a large amount of energy is wasted. The SCR catalyst is easy to block and inactivate, ammonia needs to be sprayed excessively to improve the denitration efficiency, so that vicious circle is formed, ammonia escape is further increased, the generation of sulfate, nitrate and PM2.5 in the atmosphere is aggravated, and the purification effect is poor. Therefore, it is urgent to find an economical and effective method for reducing the content of sulfur dioxide and nitrogen oxides in the sintering flue gas.
Disclosure of Invention
The invention discloses a clinker production device, which solves the problems of large volume, high energy consumption and poor purification effect of the existing equipment for desulfurization and denitrification.
The invention discloses a clinker production device, which comprises: the conveying mechanism is used for conveying the clinker; the smoke exhaust pipeline is arranged below the conveying mechanism and used for exhausting smoke generated by the clinker; the spraying device is used for spraying a purifying agent to the smoke in the smoke exhaust pipeline, and the purifying agent is used for reacting with any one or more of sulfur dioxide, sulfur trioxide and nitrogen oxide in the smoke; along the moving direction of the conveying mechanism, the clinker production device is provided with a first area and a second area, the mass concentration of sulfur dioxide in the flue gas of the second area is higher than that of the first area, and the spraying device is used for spraying a purifying agent on the flue gas generated by the second area. .
Further, the spraying device comprises: the first spray head is arranged in the smoke exhaust pipeline; the storage box is used for storing a powdery purifying agent; one end of the material conveying pipe is communicated with the first spray head, and the other end of the material conveying pipe is communicated with the material storage box; and the gas source is communicated with the material conveying pipe and is used for providing gas flow, and the purifying agent is sprayed out from the first spray head under the action of the gas flow.
Further, the spraying device further comprises: the second spray head is arranged adjacent to the first spray head, and the first spray head and the second spray head have the same direction; and the infusion tube is communicated with the second spray head and is used for conveying the reaction liquid to the second spray head (35).
Further, the clinker production device further comprises: the dust removal device is communicated with an outlet of the smoke exhaust pipeline and is provided with a filter screen, and the filter screen is used for collecting powdery substances in smoke.
Further, the spraying device comprises: the first spray head is arranged in the smoke exhaust pipeline; the liquid storage tank is used for storing a purifying agent of liquid; one end of the material conveying pipe is communicated with the first spray head, and the other end of the material conveying pipe is communicated with the material storage box; and the purifying agent is sprayed out from the first spray head under the action of the pump.
Further, the clinker production device further comprises: and the liquid collecting tank is arranged at the bottom of the smoke exhaust pipeline and is used for collecting the liquid in the smoke exhaust pipeline.
Furthermore, a flow guide surface is arranged at the bottom of the smoke exhaust pipeline and used for guiding liquid to the liquid collecting pool.
Further, the purifying agent comprises any one or more of calcium oxide, magnesium carbonate, caustic soda, sodium bicarbonate, sodium carbonate, calcium carbonate, sodium hypochlorite, hydrogen peroxide and calcium hypochlorite.
Further, the direction of the purifying agent sprayed by the spraying device is opposite to the flowing direction of the smoke in the smoke exhaust pipeline.
Further, the inner surface of the smoke exhaust pipeline is coated with an anticorrosive coating.
According to the clinker production device, the spraying device is arranged in the high-temperature area of the existing exhaust pipeline, the purifying agent can be sprayed to the flue gas in the exhaust pipeline through the spraying device, and the purifying agent can react with any one or more of sulfur dioxide, sulfur trioxide and nitrogen oxide in the flue gas, so that the flue gas is desulfurized and denitrated, large-scale equipment is not additionally arranged, the problem of sulfur dioxide, sulfur trioxide and nitrogen oxide in the sintering flue gas is integrally solved, and the flue gas is not additionally heated due to high temperature of the flue gas, so that the energy is saved.
Drawings
FIG. 1 is a schematic structural view of a clinker production apparatus according to a first embodiment of the present invention;
FIG. 2 is a schematic view of a clinker production apparatus according to a second embodiment of the present invention;
legend: 10. a transport mechanism; 20. a smoke exhaust duct; 30. a spraying device; 31. a first nozzle; 32. a material storage box; 33. a delivery pipe; 34. a liquid storage tank; 40. a dust removal device; 50. a liquid collecting tank; 60. an exhaust fan.
Detailed Description
The present invention is further illustrated by the following examples, but is not limited to the details of the description.
Among the prior art, usually collect the back through the flue gas in discharge flue with each bellows, through pipeline entering centralized processing in the SOx/NOx control equipment, this can lead to two problems: 1. after the flue gas is collected, the volume of the desulfurization equipment is large due to large amount of the flue gas, and the working pressure is huge; 2. because the proportion of sulfur dioxide is very low, the desulfurization rate is low; 3. the temperature is reduced after the flue gas is discharged, and the reaction temperature cannot be reached, so that the flue gas needs to be heated again, and the energy consumption is high.
In order to solve the problems, the invention discloses a clinker production device, which comprises a transportation mechanism 10, a smoke exhaust pipeline 20 and a spraying device 30, wherein the transportation mechanism 10 is used for transporting clinker; the smoke exhaust pipeline 20 is arranged below the transportation mechanism 10, and the smoke exhaust pipeline 20 is used for exhausting smoke generated by clinker; the spraying device 30 is used for spraying a purifying agent to the flue gas in the smoke exhaust pipeline 20, wherein the purifying agent is used for reacting with any one or more of sulfur dioxide, sulfur trioxide and nitrogen oxide in the flue gas; in the direction of movement of the transport means 10, the clinker production plant has a first zone and a second zone, the second zone having a higher mass concentration of sulphur dioxide in the flue gas than the first zone, and the spraying device 30 is used to spray cleaning agent on the flue gas generated in the second zone.
According to the clinker production device, the existing exhaust flue 20 is utilized, the spraying device 30 is arranged, the purifying agent can be sprayed to the flue gas in the exhaust flue 20 through the spraying device 30, the purifying agent can react with any one or more of sulfur dioxide, sulfur trioxide and nitrogen oxide in the flue gas, so that the flue gas is desulfurized and denitrated, no large-scale equipment is additionally arranged, the problem of sulfur dioxide, sulfur trioxide and nitrogen oxide in the sintering flue gas is integrally solved, and the flue gas is not additionally heated due to the high temperature of the flue gas, so that the energy is saved.
It should be noted that the temperature change rule and the pollutant discharge rule are as follows: flue gas temperature and SO 2 The mass concentration shows obvious 3 stages along with the change of the bellows, the first stage is a low-temperature stage of flue gas, namely when clinker is sintered in a first area, at the moment, the flue gas temperature corresponding to each bellows in the first area is 50-80 ℃, the flue gas temperature is relatively stable, the change range is small, and meanwhile SO in the flue gas is small 2 The mass concentration is very low, even 0; the second stage is a rapid rising section of the flue gas temperature, namely when the clinker is sintered in the first area, the flue gas temperature rises to the highest end temperature from below 100 ℃ at a rapid speed, and simultaneously, SO 2 The mass concentration is lower than 100mg/m 3 Rise to 4000mg/m 3 The above; in the third stage, the sintering is close to the end sound, the temperature of the flue gas is reduced, and SO 2 The mass concentration rapidly decreases after reaching the highest point.
The sulfur dioxide in the sintering flue gas is concentrated and separated out in the second area, and taking a common sintering machine commonly adopted in the field as an example, 22 wind boxes are provided, the wind boxes in the first area are provided with numbers of 1-14, and the remaining 8 wind boxes are respectively arranged in the second area and the third area, namely, the sulfur dioxide content in the first 14 wind boxes is basically absent, the flue gas entering the flue from the first 14 wind boxes occupies about 3/5 of the total flue gas, and the mixture of the flue gas in the first area, the flue gas in the second area and the flue gas in the third area can cause the proportion of the sulfur dioxide to be greatly reduced, so the flue gas amount treated by the desulfurization unit arranged outside the flue gas exhaust pipeline can be very large
That is, the clinker production plant of the present invention locates the spraying device 30 at the interface of the second zone and the first zone so as to spray the cleaning agent on the flue gas generated in the second zone. Through setting up sprinkler 30 in first region and the regional juncture of second, the realization carries out accurate desulfurization to the flue gas, the flue gas to the second region is desulfurized, not only can reduce the total amount of handling the flue gas (reduce the flue gas of first region 3/5), moreover, also make the content of sulfur dioxide in the flue gas improve, make the sulfur dioxide also improve with the reaction efficiency of decontaminating agent, the pressure of equipment operation has not only been reduced, reduce the energy consumption and hang down, can not occupy the land yet, the desorption efficiency of pollutant in the flue gas can be promoted greatly in the synthesis.
In addition, NOx is also present in the flue gas in the first zone, and sulfite, an intermediate product of the reaction of sulfur dioxide and the purification material, can be utilized as a reducing agent for denitration. After the sulfur dioxide in the second area reacts with the purifying substance, the generated sulfite is brought into the first area and can continuously react with the nitrogen oxide generated in the first area, thereby being beneficial to the removal of the nitrogen oxide. Moreover, the concentration of sulfur dioxide generated in the sintering production process is about 1500mg/m 3 About 300mg/m of nitrogen oxide 3 On the other hand, the intermediate sulfite is sufficient.
In the first embodiment shown in fig. 1, the spraying device 30 comprises a first spraying head 31, a storage tank 32, a material conveying pipe 33 and an air source, wherein the first spraying head 31 is arranged in the smoke exhaust pipe 20; the storage tank 32 is used for storing a powdery purifying agent; one end of the material conveying pipe 33 is communicated with the first nozzle 31, and the other end is communicated with the material storage box 32; the air source is communicated with the material conveying pipe 33 and is used for providing air flow, and under the action of the air flow, the purifying agent is sprayed out from the first spray head 31. The gas source inputs high-pressure airflow into the material conveying pipe 33 to enable negative pressure to be formed in the material conveying pipe 33, under the action of the negative pressure, the powdery purifying agent in the material storage box 32 is sucked into the material conveying pipe 33 and sprayed out along with the high-speed airflow, and the sprayed powdery purifying agent and sulfur dioxide, sulfur trioxide and nitrogen oxide in the flue gas are subjected to oxidation-reduction reaction, so that the aims of desulfurization and denitrification are fulfilled.
The spraying device 30 further comprises a second spray head 35 and a liquid conveying pipe, the second spray head 35 is arranged adjacent to the first spray head 31, and the first spray head 31 and the second spray head 35 are in the same direction; the liquid transport tube is communicated with the second nozzle 35, and the liquid transport tube is used for transporting the reaction liquid to the second nozzle 35. When the device is used, the first spray head 31 and the second spray head 35 spray the purifying agent and the reaction liquid to the flue gas simultaneously, so that the reaction can be promoted to be completed faster, the reaction temperature with the flue gas can be adjusted, and the desulfurization and denitrification effects are improved.
The reaction solution may be water or an oxidizing agent, and the oxidizing agent may oxidize nitric oxide into higher nitrogen oxides, and the higher nitrogen oxides may be absorbed by the purifying agent. The purifying agent comprises any one or more of calcium oxide, magnesium carbonate, caustic soda, sodium bicarbonate, sodium carbonate, calcium carbonate, sodium hypochlorite, hydrogen peroxide and calcium hypochlorite, and can react with any one or more of sulfur dioxide, sulfur trioxide and nitrogen oxide, so that the effects of desulfurization and denitrification are achieved.
The clinker production device further comprises a dust removal device 40 which is communicated with the outlet of the smoke exhaust pipeline 20, and the dust removal device 40 is provided with a filter screen which is used for collecting powdery substances in smoke. The dust removing device 40 can collect powdery substances in the flue gas, the powdery substances comprise products of the cleaning agent after reacting with the flue gas and the cleaning agent which does not react with the flue gas, and the powdery substances can be recycled, so that the utilization rate of the cleaning agent is improved.
In the second embodiment shown in fig. 2, the structure is substantially the same as that of the first embodiment, except that the spraying device 30 comprises a first nozzle 31, a liquid storage tank 34, a material conveying pipe 33 and a pump, wherein the first nozzle 31 is arranged in the smoke exhaust pipe 20; the reservoir 34 is for storing a liquid decontaminant; one end of the material conveying pipe 33 is communicated with the first nozzle 31, and the other end is communicated with the material storage box 32; the water pump is arranged on the material conveying pipe 33, and the purifying agent is sprayed out from the first spray head 31 under the action of the water pump. The liquid purifying agent can be sprayed out of the first nozzle 31 by adopting a pump, and the sprayed liquid purifying agent and sulfur dioxide, sulfur trioxide and nitrogen oxide in the flue gas are subjected to oxidation-reduction reaction, so that the aims of desulfurization and denitrification are fulfilled.
In this embodiment, the clinker production apparatus further includes a liquid collecting tank 40, the liquid collecting tank 40 is disposed at the bottom of the smoke exhaust duct 20, the liquid collecting tank 40 is used for collecting the liquid in the smoke exhaust duct 20, the liquid in the smoke exhaust duct 20 includes the product of the reaction between the purifying agent and the smoke and the purifying agent which does not react with the smoke, and the unreacted purifying agent can be recycled by recycling the liquid, so as to improve the utilization rate of the purifying agent.
Further, the bottom of the smoke exhaust pipe 20 is provided with a flow guide surface for guiding the liquid to the liquid collecting tank 40. The liquid in the smoke exhaust pipeline 20 can be more easily concentrated in the liquid collecting pool 40 by arranging the flow guide surface, so that the collecting efficiency is improved.
In the prior art, tail end pollution treatment processes such as an activated carbon (coke) method or an SCR method are commonly adopted for denitration of sintering machines. In the process, a large amount of energy is wasted in the flue gas heating process of the SCR process, and heavy metal is used as a catalyst and ammonia water is used as a reducing agent. Wherein the catalyst can form solid hazardous waste, and the ammonia escape is serious; the activated carbon (coke) removal technology also adopts ammonia water as a reducing agent, and the problem of secondary pollution caused by ammonia escape can also exist.
In order to solve the above problems, the cleaning agent is sodium bicarbonate powder or sodium bicarbonate solution. By using sodium bicarbonate powder or sodium bicarbonate solution, no hazardous waste is generated during the reaction, and no additional heating of the flue gas is required due to the temperature in the flue gas duct 20 being between 120 and 300 ℃. Sulfur dioxide, sulfur trioxide and nitrogen oxides in the flue gas can undergo redox reaction with sodium bicarbonate.
Sodium bicarbonate decomposes at high temperature to produce sodium carbonate, water and carbon dioxide. The newly produced sodium carbonate has high reactivity at the moment of generation and can spontaneously react with acidic pollutants in the flue gas in the following way. Typically, the flue gas temperature is between 120 and 300 ℃. The reaction principle is as follows:
SO 2 +NaHCO 3 →Na 2 SO 3 +CO 2 +H 2 O
Na 2 SO 3 +NO→Na 2 SO 4 +N 2
in addition, the sodium bicarbonate is used as the treatment raw material of sulfur dioxide and nitrogen oxide, and the intermediate product of the sodium bicarbonate and the sulfur dioxide is used as the raw material for removing the nitrogen oxide. Sodium bicarbonate can be rapidly decomposed into sodium carbonate at high temperature, and the whole decomposition process can expand rapidly like popcorn. Micropores are formed inside the sodium carbonate in the whole expansion process, which is more favorable for the contact of flue gas to promote the removal of pollutants.
It is noted that the purifying agent can also be an alkali liquor, and is combined with an oxidant to carry out desulfurization and denitrification. The purifying agent comprises any one or more of calcium oxide, magnesium carbonate, caustic soda, sodium bicarbonate, sodium carbonate, calcium carbonate, sodium hypochlorite, hydrogen peroxide and calcium hypochlorite, and can react with any one or more of sulfur dioxide, sulfur trioxide and nitrogen oxide, so that the effects of desulfurization and denitrification are achieved.
In order to improve the reaction effect, the spraying device 30 sprays the purifying agent in a direction opposite to the flowing direction of the flue gas in the exhaust duct 20.
It should be noted that, in the whole sintering reaction process, the exhaust duct 20 exhausts air through a plurality of bellows under the driving of the exhaust fan 60 to complete the whole reaction process. The first three fifths of the plurality of windboxes are located in the first zone and are relatively low in temperature, and the content of sulfur dioxide in the flue gas is very low, even 0. And the last two fifths of the bellows are located in the second zone in which the first nozzles 31 are arranged. As shown in FIGS. 1 and 2, a flue gas exhaust duct 20 is located below the windboxes and communicates with each windbox, both of which are in the optimum range when the temperature is to be raised, just when the evolution of sulfur dioxide begins, at the time of selection of the injection position.
In particular, it relates toThe sintering flue gas is driven by the exhaust fan and is discharged after being gathered to the flue by each bellows. Scholars at home and abroad study the pollutant emission value of each air box of the sintering machine and detect the change rule of pollutants and temperature along with different air boxes. But effective measures for treating pollutants in the sintering process at corresponding positions are not provided according to the discharge characteristics of each air box. Taking a 360 square meter sintering machine in a certain factory as an example, the sintering machine has 22 air boxes in total, and the temperature of the air boxes and the discharge of pollutants have certain change rules on the whole (the discharge rules of other sintering machines are basically consistent with the sintering machine). The flue gas temperature shows 3 obvious stages along with the change of the air boxes, wherein the first stage is a low-temperature stage of the flue gas, namely a first area, the flue gas temperature corresponding to each air box in the first area is 50-80 ℃, the flue gas temperature is relatively stable, the change range is small, and the flue gas temperature corresponds to No. 1-No. 14 air boxes of the air boxes in the first area respectively; the second stage is a rapid rising section of the flue gas temperature, namely a second area, the flue gas temperature in the second area rises from below 100 ℃ to the highest end point temperature at a relatively rapid speed, and 5-6 air boxes are arranged in the second area; the third area is a descending stage of the temperature of the flue gas, and the third area is the last 2 windboxes. SO (SO) 2 The change in mass concentration goes through 3 stages. The first area is a low-concentration section, and SO in flue gas in the first area 2 The mass concentration is very low, even 0. The bellows body is the bellows from No. 1 to No. 14; the second area is a fast rising section, and the number of the wind boxes in the area is 4-5 SO 2 The mass concentration is lower than 100mg/m 3 Rise to 4000mg/m 3 Above, the third region is a fast descending segment, and this region is SO 2 The mass concentration rapidly decreases after reaching the highest point. NO X The change trend of the mass concentration is also divided into 3 stages, namely a rapid rising stage, a high concentration stage, a rapid falling stage and the like, wherein in the first stage, NO in the flue gas X The mass concentration rises rapidly, and the stage is mainly concentrated on No. 1-No. 4 bellows; the second stage is a high concentration stage with mass concentration of 200mg/m 3 The air boxes are mainly concentrated on No. 5 to No. 15 air boxes on two sides; the third stage is a rapid descent stage, in which stage NO X From a high concentration to almost 0. This application is madeThe patent selects the position before the sulfur dioxide begins to rise, the temperature of the position is suitable for removing pollutants, and the amount of flue gas to be treated is small.
It should be noted that, since water meets SOx and nitrogen oxides to form an acidic solution, in order to avoid the acidic solution to corrode the inside of the smoke exhaust pipe, the inner surface of the smoke exhaust pipe is coated with an anticorrosive coating, for example: glass flake anticorrosive coating. The inner surface of the smoke exhaust pipeline is coated with the anticorrosive coating, so that the inner surface of the smoke exhaust pipeline can be prevented from being corroded by acid such as sulfurous acid, sulfuric acid and the like, and the running reliability of equipment is improved.
It should be understood that the above-described embodiments of the present invention are merely examples for clearly illustrating the present invention and are not intended to limit the present invention. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. Not all embodiments are exhaustive. All obvious changes and modifications which are obvious to the technical scheme of the invention are covered by the protection scope of the invention.
Claims (10)
1. A clinker production apparatus, characterized by comprising:
a transport means (10) for transporting the clinker;
the smoke exhaust pipeline (20) is arranged below the conveying mechanism (10), and the smoke exhaust pipeline (20) is used for exhausting smoke generated by the clinker;
a spraying device (30) for spraying a purifying agent to the flue gas in the smoke exhaust pipeline (20), wherein the purifying agent is used for reacting with any one or more of sulfur dioxide, sulfur trioxide and nitrogen oxide in the flue gas;
along the moving direction of the conveying mechanism (10), the clinker production device is provided with a first area and a second area, the mass concentration of sulfur dioxide in the flue gas of the second area is higher than that of the first area, and the spraying device (30) is used for spraying purifying agent on the flue gas generated by the second area.
2. A clinker production plant according to claim 1, characterized in that said spraying device (30) comprises:
a first spray head (31) arranged in the smoke exhaust duct (20);
a storage tank (32) for storing a powdery purifying agent;
one end of the material conveying pipe (33) is communicated with the first spray head (31), and the other end of the material conveying pipe is communicated with the material storage box (32);
and the gas source is communicated with the material conveying pipe (33), the gas source is used for providing gas flow, and the purifying agent is sprayed out from the first spray head (31) under the action of the gas flow.
3. A clinker production device according to claim 2, characterized in that said spraying device (30) further comprises:
a second spray head (35) arranged adjacent to the first spray head (31), the first spray head (31) and the second spray head (35) being oriented in the same direction;
and the infusion tube is communicated with the second spray head (35) and is used for conveying reaction liquid to the second spray head (35).
4. A clinker production device according to claim 3, characterized in that said clinker production device further comprises:
dust collector (40), with the export intercommunication of exhaust pipe (20), dust collector (40) are provided with the filter screen, the filter screen is arranged in collecting the powdery material in the flue gas.
5. A clinker production plant according to claim 1, characterized in that said spraying device (30) comprises:
a first spray head (31) arranged in the smoke exhaust duct (20);
a reservoir (34) for storing a liquid decontaminant;
one end of the material conveying pipe (33) is communicated with the first spray head (31), and the other end of the material conveying pipe is communicated with the material storage box (32);
and the pump is arranged on the conveying pipe (33), and the purifying agent is sprayed out from the first spray head (31) under the action of the pump.
6. A clinker production device according to claim 5, characterized in that said clinker production device further comprises:
the liquid collecting pool (50) is arranged at the bottom of the smoke exhaust pipeline (20), and the liquid collecting pool (50) is used for collecting liquid in the smoke exhaust pipeline (20).
7. The clinker production apparatus of claim 6,
the bottom of the smoke exhaust pipeline (20) is provided with a flow guide surface, and the flow guide surface is used for guiding liquid to the liquid collecting pool (50).
8. The clinker production apparatus of claim 1,
the purifying agent comprises any one or more of calcium oxide, magnesium carbonate, caustic soda, sodium bicarbonate, sodium carbonate, calcium carbonate, sodium hypochlorite, hydrogen peroxide and calcium hypochlorite.
9. The clinker production apparatus of claim 1,
the spraying device (30) sprays the purifying agent in the direction opposite to the flowing direction of the smoke in the smoke exhaust pipeline (20).
10. The clinker production apparatus of claim 1,
the inner surface of the smoke exhaust pipeline (20) is coated with an anticorrosive coating.
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| CN202210509986.XA CN114797441A (en) | 2022-05-11 | 2022-05-11 | Clinker production device |
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| CN202210509986.XA CN114797441A (en) | 2022-05-11 | 2022-05-11 | Clinker production device |
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