CN210495923U - Flue gas emission purification system - Google Patents
Flue gas emission purification system Download PDFInfo
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- CN210495923U CN210495923U CN201921035558.8U CN201921035558U CN210495923U CN 210495923 U CN210495923 U CN 210495923U CN 201921035558 U CN201921035558 U CN 201921035558U CN 210495923 U CN210495923 U CN 210495923U
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Abstract
The utility model provides a flue gas emission clean system mainly includes: a water medium type flue gas heat exchanger (MGGH), a desulfurizing tower, a flue gas condenser, a rotary flue gas heat exchanger (GGH), a flue combustor/hot blast stove, an ammonia water vaporizer, a denitration device, a booster fan and a chimney. The utility model discloses an ammonia process desulfurization and selective catalytic reduction denitration (SCR) technique have realized sulfur dioxide, nitrogen oxide and the ultralow emission of particulate matter to and the purpose that the flue gas disappears whitely. The ammonia desulfurization effect is improved by an ultrasonic rotational flow atomization technology; through the washing purification section and the flue gas condensation technology, the temperature and the particulate matter content of the flue gas at the outlet after desulfurization are reduced, the water carrying amount of the flue gas is reduced, and the water consumption of a system is reduced; the energy consumption required by denitration is reduced through the rotary flue gas heat exchanger, the final temperature of flue gas emission is increased, and the white smoke elimination is realized; the process route is simple and easy to operate.
Description
Technical Field
The utility model relates to an environmental protection field, concretely relates to gas cleaning technique, especially a sintering, pelletizing aircraft nose smoke emission clean system belongs to environmental protection (gas cleaning) technical field.
Background
In the steel industry or other industrial production, flue gas generated by combustion between raw materials and fuel contains a large amount of nitrogen oxides, sulfur dioxide and particulate matters, and causes certain pollution to the atmosphere. Five committees such as the department of ecological environment of 4 months in 2019 jointly issue an opinion on promoting implementation of ultra-low emission in the steel industry, and clearly define the target and index of transformation. The indexes are as follows: the small-average values of the emission concentrations of the pellet machine head, pellet roasting smoke particles, sulfur dioxide and nitrogen oxides are respectively not higher than 10 mg/cubic meter, 35 mg/cubic meter and 50 mg/cubic meter (the reference oxygen contents of the sintering machine head and the pellet shaft furnace are 16%, and the reference oxygen contents of the grate rotary kiln and the belt type pellet roasting machine are 18%); the hourly mean values of the emission concentrations of the other main pollution sources of particulate matters, sulfur dioxide and nitrogen oxides are respectively not higher than 10, 50 and 200 mg/cubic meter in principle.
The method for removing sulfur dioxide in sintering and pelletizing flue gas in the steel industry mainly comprises a wet method, a dry method and a semi-dry method, wherein the wet method mainly comprises a limestone-gypsum method, an ammonia method, a magnesium oxide method, a double-alkali washing method and the like. The mature and widely applied sintering and pelletizing machine head fume wet desulfurizing technology is calcium process and ammonia process, wherein the ammonia process desulfurizing efficiency can reach over 98%, ammonia water is used as desulfurizing agent and (NH) is used4)2SO3、(NH4)2SO4、NH3HSO3To circularly absorb SO2Thereby achieving removal of SO2The purpose of (1). The desulfurized flue gas is washed, purified and washed by water, and liquid drops and particulate matters contained in the flue gas are captured by means of dedusting, demisting, flue gas condensation and the like, the water content is reduced, and the ultralow emission of sulfur dioxide and particulate matters is realized. And (3) enabling the ammonium sulfate solution with a certain concentration obtained in the desulfurization process to enter an ammonium sulfate preparation system, and obtaining the finished ammonium sulfate fertilizer through processes of evaporation, crystallization, drying and the like.
The removal method of nitrogen oxides mainly includes a reduction method, an oxidation method and a decomposition method. Selective non-catalytic reduction (SNCR) and Selective Catalytic Reduction (SCR) in reduction processes are considered the most effective denitration techniques, and are able to meet stringent flue gas emission standards. At present, the sintering and pelletizing head flue gas temperature of steel enterprises is generally 120-160 ℃, the temperature ranges of selective non-catalytic reduction (SNCR) and Selective Catalytic Reduction (SCR) reaction windows are not in any condition, but the pellet flue gas temperature can be increased to 200-320 ℃ by a afterburning device/hot blast stove and a rotary flue gas heat exchanger with less energy consumption, so that the low and medium temperature SCR reaction window temperature is reached. Under the condition of the temperature, a reducing agent ammonia is sprayed into the flue gas, the ammonia reacts with the nitrogen oxide in the flue gas under the action of a catalyst to generate non-toxic and pollution-free nitrogen and water, so that ultralow emission of the nitrogen oxide is realized, and meanwhile, the rotary flue gas heat exchanger can improve the temperature of the discharged flue gas to 95-130 ℃ to realize the whitening effect of the discharged flue gas. The sintering and pelletizing head smoke emission purification system realizes the ultralow emission of sulfur dioxide, nitrogen oxide and particulate matters and the whole process of smoke whitening, the byproduct is ammonium sulfate fertilizer, no waste water, waste residue and waste gas are generated, and the system belongs to an environment-friendly means of green and circular economy.
SUMMERY OF THE UTILITY MODEL
The utility model provides a flue gas emission clean system mainly adopts ammonia process desulfurization and selective catalytic reduction denitration (SCR) technique to realize flue gas sulfur dioxide, nitrogen oxide and the ultralow emission of particulate matter, and the flue gas disappears and whitens as the purpose.
Therefore, the utility model provides a (sintering, pelletizing aircraft nose) fume emission clean system, fume emission clean system includes:
the water medium type flue gas heat exchanger (MGGH) is provided with a temperature rising section and a temperature reducing section, the temperature reducing section is arranged on a flue from the main exhaust fan to the inlet of the desulfurizing tower, and the temperature reducing section is connected with the flue behind the pellet main exhaust fan; the temperature rising section is arranged on a flue from an outlet of the desulfurizing tower to an inlet (a first inlet) at the raw flue gas side of the rotary flue gas heat exchanger, and the temperature rising section is connected with the rotary flue gas heat exchanger.
The desulfurizing tower is connected with the cooling section of the hydrophily type flue gas heat exchanger;
the flue gas condenser is connected with the desulfurizing tower;
the temperature rising section of the hydrophily type flue gas heat exchanger is connected with the flue gas condenser;
the rotary flue gas heat exchanger is provided with a raw flue gas side inlet (a first inlet), a raw flue gas side outlet (a first outlet), a purified flue gas inlet (a second inlet) and a purified flue gas side outlet (a second outlet), and the raw flue gas side inlet of the rotary flue gas heat exchanger is connected with the temperature rising section of the hydrophily flue gas heat exchanger;
the flue combustor/hot blast stove is arranged in a flue at the original flue gas side outlet of the rotary flue gas heat exchanger; or a hot blast stove is connected to a flue at the original flue gas side outlet of the rotary flue gas heat exchanger;
the ammonia water vaporizer is connected to the original flue gas side outlet flue of the rotary flue gas heat exchanger;
the denitration reactor is connected with the raw flue gas side outlet flue;
the second inlet of the rotary flue gas heat exchanger is connected with the denitration reactor;
the booster fan is connected with the second outlet of the rotary flue gas heat exchanger;
the clean flue gas inlet of the rotary flue gas heat exchanger is connected with the denitration reactor;
the clean smoke outlet of the rotary smoke heat exchanger is connected with the clean smoke inlet of the rotary smoke heat exchanger;
the booster fan is connected with the clean smoke side outlet of the rotary smoke heat exchanger;
and the chimney is connected with the outlet of the booster fan.
Further, the desulfurization tower includes: 1 section of independent circulating cooling and concentrating section, the running density index is 1.15-1.18g/cm3The discharge density index is 1.20-1.30g/cm3(ii) a 1-2 sections of independently circulating absorption sections, and the running density index is 1.05-1.11g/cm3(ii) a 1-3 sections of independent circulating water washing purification sections with the operation density index of 1.01-1.03g/cm3(ii) a The system adopts ammonia water as the total liquid-gas ratio which is more than or equal to 9, and a high-efficiency demister is arranged between each independent circulation section to avoid slurry entrainment.
Further, the desulfurization system includes: and the plurality of cyclone atomizers are arranged on the side wall of the cooling concentration section or the absorption section of the desulfurizing tower, and the particle size of the desulfurizing slurry sprayed by the atomizers is 50-150 mu m.
Further, the plurality of cyclone atomizers are arranged on the side wall of the desulfurizing tower in the tangential direction of the same horizontal plane.
Further, a rotational flow spray layer is formed by a plurality of rotational flow atomizers arranged on the side wall of the desulfurizing tower and tangential to the same horizontal plane. When the rotational flow atomizer is arranged for coolingDuring the concentration section, on one hand, the particle size of the desulfurizer is reduced to 50-150 mu m from 1500-3000 mu m of the traditional spray layer, and the specific surface area of the equivalent desulfurization slurry particles is increased by more than 400-900 times, so that the desulfurization absorption specific surface area is increased, the reaction speed is accelerated, the high-efficiency desulfurization under the condition of small liquid-gas ratio is realized, and the desulfurization energy consumption is reduced; on the other hand, because the atomization rotational flow tangent circle arrangement technology is adopted, a spray rotational flow field in the desulfurizing tower is constructed to form a high-speed rotating cloud shape, the flue gas and the desulfurizing agent are fully and uniformly mixed, and SO in the flue gas is increased2The reaction probability with the desulfurizer improves the desulfurization efficiency. The rotational flow spraying layer not only has the function of a reverse flow spraying layer, but also has the function of high-efficiency turbulent flow reaction. The cloud flow field reconstruction is realized, a stable rotating air film stabilizing layer in the desulfurizing tower is formed, the problem of a flue gas corridor in a conventional spray tower is solved, the cooling, dedusting and desulfurizing efficiency is further improved, and the generation of aerosol is reduced.
Further, the water-borne flue gas heat exchanger further comprises: the cooling section and the heating section both adopt a corrosion-resistant steel H-shaped fin form; the cooling section is arranged on a front flue of the desulfurizing tower and used for reducing the temperature of the flue gas at the inlet of the desulfurizing tower by 30-40 ℃; and the temperature rise section is arranged behind the flue gas condenser, and the temperature of the flue gas at the outlet of the desulfurizing tower is raised by 30-40 ℃.
① reducing the temperature of the slurry by 5-10 ℃ through a slurry heat exchanger (plate or tube corrosion resistant steel heat exchanger) arranged at a cooling concentration section/absorption section/washing purification section, cooling the desulfurized flue gas to 45-48 ℃ through spraying the cooled slurry, ② condensing the desulfurized flue gas through an independent condenser (adopting fluoroplastic or corrosion resistant steel) arranged on a flue at the outlet of the desulfurizing tower, directly cooling and condensing the desulfurized flue gas from 53-55 ℃ to 45-48 ℃, wherein the flue gas condenser adopts one of the 2 schemes.
Furthermore, when the flue gas passes through the condensation dust removal demister, the temperature is reduced by 5-10 ℃, the water carrying rate of saturated flue gas is reduced, the water consumption of a system is reduced, and the protection of rear-end denitration GGH and the whitening of the flue gas are facilitated.
Further, the denitration device is arranged after the desulfurization tower.
Further, the denitration device further comprises: the catalyst adopts a wide temperature plate type or a honeycomb type, and the bed layer is designed into a 2+1 or 3+1 mode.
Further, the denitration device further comprises: the design and adjustment range of the denitration reaction temperature is 200-320 ℃, and the method has good adaptability.
Further, the rotary flue gas heat exchanger also comprises: the smoke temperature of the clean smoke outlet of the rotary smoke heat exchanger reaches 95-130 ℃, and smoke whitening is realized.
Further, the booster fan is arranged behind the denitration device, and the booster fan adopts an axial flow type.
The utility model discloses better combine Selective Catalytic Reduction (SCR) denitration technique with ammonia process desulfurization technology, adopt the process route of denitration after earlier desulfurization. The MGGH is matched with the cyclone atomizer to reduce the temperature of the flue gas in the tower, so that ammonia desulphurization control is facilitated, the desulphurization efficiency is improved, ammonia escape is reduced, the temperature of the flue gas behind a flue gas condenser is improved, and denitration GGH is protected from corrosion; the flue gas condenser is utilized to further reduce the temperature and the water content of the desulfurized saturated flue gas, so that the water consumption of the system is reduced; by using denitration GGH, the desulfurized sintering and pelletizing flue gas is lifted to the temperature of a selective catalytic reduction denitration reaction window with low energy consumption, the final emission temperature of the denitrated flue gas is increased, and the whitening of the flue gas is realized. The whole device has simple process route and easy operation, and is a great breakthrough in the fields of sintering and pellet flue gas purification for technologies of energy conservation, emission reduction, environmental protection, byproduct recycling and the like.
Drawings
Fig. 1 is a schematic view of the working principle of the present invention.
1. Sintering and pelletizing main exhaust fan; 2. a hydrophily type flue gas heat exchanger (a cooling section); 3. a hydrophily type flue gas heat exchanger (a temperature rising section); 4. a desulfurizing tower (comprising a rotational flow atomizing nozzle and multi-section circulation); 5. a flue gas condenser; 6. GGH; 7. hot blast stove/flue burners; 8. a denitration device (containing a catalyst); 9. a booster fan; 10. and (4) a chimney.
Detailed Description
In order to clearly understand the technical features, objects and effects of the present invention, the present invention will now be described with reference to the accompanying drawings.
The technical principle of the utility model
The desulfurization principle is as follows:
NH3+SO2+H2O＝NH4HSO3
2NH3+SO2+H2O＝(NH4)2SO3
(NH4)2SO3+SO2+H2O＝2NH4HSO3(desulfurization main reaction)
NH4HSO3+NH3＝(NH4)2SO3
The denitration principle is as follows:
4NO+4NH3+O2→4N2+6H2O
2NO2+4NH3+O2→3N2+6H2O
① the flue gas heat exchanger (MGGH) transfers the flue gas heat of the sintering and pelletizing head at the desulfurization inlet to the clean flue gas after desulfurization, thereby achieving the effects of reducing the flue gas temperature at the desulfurization inlet and improving the flue gas temperature at the desulfurization outlet;
① the circulating slurry of the cooling concentration section/absorption section/washing purification section is cooled by a slurry heat exchanger (plate or tube corrosion resistant steel heat exchanger), the cooled circulating slurry is sprayed to cool the desulfurization flue gas, ② the flue gas at the outlet of the desulfurization tower is directly condensed and cooled by an independent condenser (tube heat exchange element made of fluoroplastic or corrosion resistant steel).
Furthermore, when the flue gas passes through the condensation dust removal demister, the temperature is reduced by 5-10 ℃, the water carrying rate of saturated flue gas is reduced, the water consumption of a system is reduced, and the protection of rear-end denitration GGH and the whitening of the flue gas are facilitated.
The utility model discloses utilize ammonia process desulfurization, selective catalytic reduction denitration technique to reduce and rise each functional area's flue gas temperature through hydrophily formula gas heater and rotation gas heater, realize sintering, pelletizing aircraft nose flue gas sulfur dioxide, nitrogen oxide and remove the particulate matter ultra-clean emission under lower energy consumption condition.
The utility model discloses the concrete process of realization: as shown in figure 1 of the drawings, in which,
(1) a rotary flue gas heat exchanger (GGH) (rotary flue gas heat exchanger 5) is arranged at the downstream of the denitration device (containing catalyst) 7;
(2) sintering and pelletizing raw flue gas (120-;
(3) the flue gas is subjected to temperature reduction, dust removal and desulfurization absorption with common desulfurization slurry (the grain diameter is 1500-3000 mu m) and rotational flow atomization desulfurization slurry (the grain diameter is 50-150 mu m) in a desulfurization tower, and then after 1-3-stage water washing, the temperature of the desulfurized flue gas is further reduced to 45-48 ℃ through a flue gas condenser, so that the water carrying capacity of saturated flue gas is reduced, and a secondary deep dust removal function is also provided. And (4) oxidizing and concentrating the slurry obtained by desulfurization, then sending the slurry to an ammonium sulfate preparation system, and preparing an ammonium sulfate finished product by adopting the processes of evaporation, crystallization, drying and the like.
(4) And (3) enabling the purified desulfurization flue gas treated by the desulfurization tower to enter a temperature rise section 4 of the water-borne flue gas heat exchanger, raising the temperature of the purified desulfurization flue gas by 30-40 ℃, and changing the purified desulfurization flue gas from a saturated state to an unsaturated state.
(5) The desulfurized clean flue gas heated by the hydrophily type flue gas heat exchanger enters a rotary flue gas heat exchanger (denitration raw flue gas side) 5 to exchange heat with flue gas (200-;
(3) the denitration original flue gas after heat exchange and temperature rise of the rotary flue gas heat exchanger is heated to 200-320 ℃ through a hot blast stove or a afterburning device 6, and then is uniformly mixed with the ammonia-containing flue gas from a dilution fan;
(4) denitration raw smoke uniformly mixed with ammonia gasThe gas enters a denitration device 7, and under the active catalytic action of a wide-temperature catalyst in the denitration device, the ammonia gas converts NOXReduction to N2And H2O, realizing the removal function of nitrogen oxides;
(5) the denitrated high-temperature denitrated clean flue gas (200-;
(6) the denitrated clean flue gas after cooling enters the booster fan 8, and the booster fan 8 can overcome the resistance of the whole system.
(7) The denitrified clean flue gas after passing through the booster fan 8 is discharged into the atmosphere through a chimney 9, and no obvious white smoke phenomenon exists.
The utility model discloses in, each stage technical essential:
(1) the process route of firstly desulfurizing and then denitrifying is adopted by combining ammonia desulfurization and Selective Catalytic Reduction (SCR) denitration technology.
(2) ① adopts high-efficiency ammonia desulfurization technique, the by-product is ammonium sulfate fertilizer, no waste water and waste are generated in the whole production process, and resource utilization of the by-product is realized. ② selects high-efficiency cyclone atomizer to carry out cooling dedusting or desulfurization in the tangential circle arrangement in the tower, a cyclone spray layer is formed on the plane of the desulfurization tower, the particle size of the desulfurization slurry is reduced to 50-150 μm from the common 1500-fold 3000 μm, the specific surface area of the same desulfurization slurry is increased by 400-900 times, the desulfurization absorption specific surface area is increased, the reaction speed is accelerated, the cyclone spray layer has the function of high-efficiency turbulent reaction, the cloud flow field reconstruction is realized, a stable rotating air film stabilizing layer in the desulfurization tower is formed, the problem of flue gas corridor in the conventional spray tower is solved, the cooling, dedusting and desulfurization efficiencies are further improved. ③ the desulfurization tower is provided with 1 section of independently circulating cooling and concentrating section, and the operation density index is 1.15-1.18g/cm3The discharge density index is 1.20-1.30g/cm3(ii) a 1-2 sections of independently circulating absorption sections, and the running density index is 1.05-1.11g/cm3(ii) a 1-3 sections of independent circulating water washing purification sections with the operation density index of 1.01-1.03g/cm3(ii) a The total liquid-gas ratio of the system is more than or equal to 9, and a high-efficiency demister is arranged between each independent circulation section to avoid slurry entrainment.
(3) ① adopts high-efficiency selective catalytic reduction denitration technology (SCR), byproducts are nitrogen and water, no other waste water and waste are generated, ② selects wide-temperature catalyst with better adaptability, the normal reaction temperature range is 200-320 ℃, a plate type or honeycomb type can be adopted, the bed layer is designed into a 2+1 or 3+1 mode, and the phenomena of blockage, poisoning and inactivation of the catalyst are avoided.
(4) ②, high-temperature sintering after denitration is carried out through a rotary flue gas heat exchanger (GGH), and the heat of the flue gas of the pellet clean machine head is transferred to the sintering of the denitration inlet and the raw flue gas of the pellet machine head, so that the effects of increasing the flue gas temperature of the denitration inlet and reducing the energy consumption of a afterburner are achieved;
(5) ① the circulating slurry of the cooling concentration section/absorption section/washing purification section is cooled by a slurry heat exchanger (plate or tube corrosion resistant steel heat exchanger), the cooled circulating slurry is sprayed to cool the desulfurization flue gas, ② the flue gas at the outlet of the desulfurization tower is condensed and cooled by an independent condenser (tube heat exchange element made of fluoroplastic or corrosion resistant steel).
The specific embodiment is as follows:
the Guangxi Steel group Limited company 2 x 500 square meter sintering and 400 ten thousand ton/year pelletizing machine head flue gas desulfurization and denitration project, the design flue gas amount is 180 x 104Nm3Per hour (one square meter, 500 square meters and sintering) and 125X 104Nm3Perh, the concentration of the particles is 50 mg/Nm3The concentration of sulfur dioxide is 2000 mg/Nm3The concentration of nitrogen oxides is 400 mg/Nm3The adopted process flow comprises the following steps: sintering and pelletizing machine head flue gas → machine head electric dust remover → main exhaust fan 1 → hydrophily type flue gas heat exchanger cooling section 2 → desulfurizing tower 4 (including cooling and dust removing, absorbing and water washing purifying, and adopting cyclone atomizer technology and the like) → flue gas condenser 5 → hydrophily type flue gas heat exchanger (MGGH) heating section 3 → rotary flue gas heat exchanger 6 (denitrified raw flue gas side) → hot blast stove/flue burner 7 → denitrator 8 →The rotary flue gas heat exchanger 6 (denitration clean flue gas side) → the booster fan 9 → the chimney 10, and the whole process realizes high-efficiency desulfurization, denitration, dust removal, defogging and whitening of flue gas by cooling and heating the flue gas twice. Preferably, the concentration of the particles discharged through the chimney is less than 10 mg/Nm3The concentration of sulfur dioxide is less than 35 mg/Nm3The concentration of nitrogen oxides is less than 50 mg/Nm3The dust removal efficiency is more than 80%, the desulfurization efficiency is more than 98.5%, the denitration efficiency is more than 87.5%, the smoke exhaust temperature is 120-125 ℃, the smoke whitening is realized, the national ultra-low emission standard is met, and meanwhile, the ammonium sulfate fertilizer byproduct is obtained, and the recycling economy of the byproduct resource is realized.
The above description is only exemplary of the present invention, and is not intended to limit the scope of the present invention. For the utility model discloses a each component can make up each other under the condition of conflict not, and any technical personnel in the field do not deviate from the utility model discloses an equal change and the modification made under the prerequisite of the design and principle all should belong to the scope of protection of the utility model.
Claims (2)
1. A flue gas emission cleaning system, characterized in that the flue gas emission cleaning system comprises:
the hydrophily type flue gas heat exchanger is provided with a temperature rising section and a temperature reducing section, wherein the temperature reducing section is arranged on a flue from a main exhaust fan to an inlet of the desulfurizing tower, and the temperature reducing section is connected with the flue behind the main exhaust fan; the temperature rising section is arranged on a flue from the outlet of the desulfurizing tower to the inlet of the original flue gas side of the rotary flue gas heat exchanger, namely the first inlet, and the temperature rising section is connected with the flue gas condenser;
the desulfurizing tower is connected with the cooling section of the hydrophily type flue gas heat exchanger;
the flue gas condenser is connected with the desulfurizing tower;
the temperature rising section of the hydrophily type flue gas heat exchanger is connected with the flue gas condenser;
the rotary flue gas heat exchanger is provided with a raw flue gas side inlet, namely a first inlet, a raw flue gas side outlet, namely a first outlet, and a clean flue gas inlet, namely a second inlet, and a clean flue gas side outlet, namely a second outlet, wherein the raw flue gas side inlet of the rotary flue gas heat exchanger is connected with the temperature rising section of the hydrophily flue gas heat exchanger;
the flue combustor/hot blast stove is arranged in a flue at the original flue gas side outlet of the rotary flue gas heat exchanger; or a hot blast stove is connected to a flue at the original flue gas side outlet of the rotary flue gas heat exchanger;
the ammonia water vaporizer is connected to the original flue gas side outlet flue of the rotary flue gas heat exchanger;
the denitration reactor is connected with the raw flue gas side outlet flue;
the second inlet of the rotary flue gas heat exchanger is connected with the denitration reactor;
the booster fan is connected with the second outlet of the rotary flue gas heat exchanger;
the clean flue gas inlet of the rotary flue gas heat exchanger is connected with the denitration reactor;
the clean smoke outlet of the rotary smoke heat exchanger is connected with the clean smoke inlet of the rotary smoke heat exchanger;
the booster fan is connected with the clean smoke side outlet of the rotary smoke heat exchanger;
and the chimney is connected with the outlet of the booster fan.
2. The flue gas emission purification system of claim 1, wherein the desulfurization tower comprises: 1 section of independent circulating cooling and concentrating section, the running density index is 1.15-1.18g/cm3The discharge density index is 1.20-1.30g/cm3(ii) a 1-2 sections of independently circulating absorption sections, and the running density index is 1.05-1.11g/cm3(ii) a 1-3 sections of independent circulating water washing purification sections with the operation density index of 1.01-1.03g/cm3(ii) a And a demister is arranged between each independent circulation section to avoid slurry entrainment.
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| CN201921035558.8U CN210495923U (en) | 2019-07-04 | 2019-07-04 | Flue gas emission purification system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110354677A (en) * | 2019-07-04 | 2019-10-22 | 柳州钢铁股份有限公司 | It is a kind of sintering, pelletizing head flue gas emission purification system |
| CN111569626A (en) * | 2020-05-22 | 2020-08-25 | 四川君和环保股份有限公司 | Sintering flue gas treatment process and system |
-
2019
- 2019-07-04 CN CN201921035558.8U patent/CN210495923U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110354677A (en) * | 2019-07-04 | 2019-10-22 | 柳州钢铁股份有限公司 | It is a kind of sintering, pelletizing head flue gas emission purification system |
| CN110354677B (en) * | 2019-07-04 | 2024-02-27 | 柳州钢铁股份有限公司 | Sintering and pelletizing machine head smoke emission purifying system |
| CN111569626A (en) * | 2020-05-22 | 2020-08-25 | 四川君和环保股份有限公司 | Sintering flue gas treatment process and system |
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