CN109813131B - Method for treating gypsum calcination flue gas - Google Patents
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Abstract
The invention relates to a method for treating gypsum calcination flue gas, which comprises the following steps: a) burning the fuel in a combustion chamber of a gypsum calciner to generate hot flue gas; fuel combustion processIn the process, spraying ammonia water into the combustion chamber; b) cooling the hot flue gas, then sending the cooled hot flue gas into a calcining chamber of a gypsum calcining furnace, and calcining gypsum powder in the cooled hot flue gas in the calcining chamber to obtain mixed flue gas; c) carrying out dry-type electric precipitation on the mixed flue gas to obtain dedusting flue gas and dust; d) oxidizing the dedusting flue gas in the presence of an oxidant to obtain oxidized flue gas; e) carrying out wet desulphurization on the oxidized flue gas to obtain desulfurized nitrate flue gas; f) and carrying out wet-type electric precipitation on the desulfurized and denitrified flue gas to obtain purified flue gas. The experimental results show that: the method can realize ultralow emission of pollutants in flue gas generated in gypsum calcination, and the concentration of particulate matters in the treated flue gas is less than or equal to 10mg/Nm3、SO2The concentration is less than or equal to 50mg/Nm3、NOXConcentration is less than or equal to 100mg/Nm3。
Description
Technical Field
The invention belongs to the field of environmental protection, and particularly relates to a method for treating gypsum calcination flue gas.
Background
Gypsum stone or industrial by-product gypsum exists in the form of calcium sulfate dihydrate, which has two crystal waters in its molecular formula, and only one semi-crystal water is removed to form calcium sulfate hemihydrate, which has gelling properties. The process of removing crystal water is gypsum calcination.
The calcining of the gypsum is mainly carried out in a gypsum calcining furnace, the calcining dehydration of the materials is mainly completed by utilizing the direct contact of the high-temperature hot flue gas and the gypsum raw material, and in the equipment, because the heat exchange is directly completed between the materials and the flue gas, the equipment has higher thermal efficiency and thermal utilization rate, high calcining speed and low production energy consumption, and is very suitable for the production of large-scale gypsum products.
In recent years, along with the rapid development of the gypsum industry, the emission of waste flue gas generated by calcining gypsum is increasing. Facing increasingly severe environmental problems, how to reduce the pollutant concentration of gypsum calcination flue gas and realize clean production of gypsum calcination is a technical problem to be solved urgently in the gypsum industry at present.
Disclosure of Invention
In view of this, the invention aims to provide a method for treating gypsum calcination flue gas, which can realize ultralow emission of flue gas pollutants and meet the requirement of clean production.
The invention provides a method for treating gypsum calcination flue gas, which comprises the following steps:
a) burning the fuel in a combustion chamber of a gypsum calciner to generate hot flue gas; in the process of burning the fuel, spraying ammonia water into the combustion chamber;
b) cooling the hot flue gas, then sending the cooled hot flue gas into a calcining chamber of a gypsum calcining furnace, and calcining gypsum powder in the cooled hot flue gas in the calcining chamber to obtain mixed flue gas;
c) carrying out dry-type electric precipitation on the mixed flue gas to obtain dedusting flue gas and dust; the dust comprises calcined gypsum powder and smoke dust;
d) oxidizing the dedusting flue gas in the presence of an oxidant to obtain oxidized flue gas;
e) carrying out wet desulphurization on the oxidized flue gas to obtain desulfurized nitrate flue gas;
f) and carrying out wet-type electric precipitation on the desulfurized nitrate flue gas to obtain purified flue gas.
Preferably, in the step a), the cooling mode of the hot flue gas is as follows:
and part of the dedusting flue gas returns to the gypsum calcining furnace to be mixed with the hot flue gas.
Preferably, the method further comprises the following steps:
and returning part of the dedusting flue gas to the gypsum calcining furnace to adjust the air surplus coefficient of the combustion chamber.
Preferably, the step a) further comprises:
and in the process of burning the fuel, lime powder is sprayed into the combustion chamber.
Preferably, in the step a), the combustion temperature is 800-950 ℃.
Preferably, in the step b), the temperature of the cooled hot flue gas is 550-650 ℃.
Preferably, in the step c), the temperature of the dedusting flue gas is 120-160 ℃.
Preferably, in step d), the oxidation is carried out in a spray tower.
Preferably, in the step e), the wet desulfurization is performed by a double-alkali desulfurization method.
Preferably, in the step e), the dual-alkali desulfurization is performed in a spray tower, and a demister is arranged at a flue gas outlet end of the spray tower.
Compared with the prior art, the inventionProvides a method for treating gypsum calcination flue gas. The processing method provided by the invention comprises the following steps: a) burning the fuel in a combustion chamber of a gypsum calciner to generate hot flue gas; in the process of burning the fuel, spraying ammonia water into the combustion chamber; b) cooling the hot flue gas, then sending the cooled hot flue gas into a calcining chamber of a gypsum calcining furnace, and calcining gypsum powder in the cooled hot flue gas in the calcining chamber to obtain mixed flue gas; c) carrying out dry-type electric precipitation on the mixed flue gas to obtain dedusting flue gas and dust; the dust comprises calcined gypsum powder and smoke dust; d) oxidizing the dedusting flue gas in the presence of an oxidant to obtain oxidized flue gas; e) carrying out wet desulphurization on the oxidized flue gas to obtain desulfurized nitrate flue gas; f) and carrying out wet-type electric precipitation on the desulfurized nitrate flue gas to obtain purified flue gas. According to the invention, aiming at the temperature requirement and the flue gas characteristics of the gypsum calcination process, the reduction method denitration (SNCR) is adopted at the high-temperature section of the flue gas, then the flue gas is cooled and the gypsum calcination is completed, then the dry-method electric precipitation is used for completing the material collection, then the oxidation denitration and the wet-method desulphurization of the low-temperature flue gas are carried out, and finally the wet-method electric precipitation is used for collecting liquid drops and particles in the flue gas, so that the ultralow emission of pollutants in the gypsum calcination flue gas is realized, and the requirement of clean production can be met. The experimental results show that: the treatment method can realize ultralow emission of pollutants in flue gas generated in gypsum calcination, and the concentration of particulate matters in the treated flue gas is less than or equal to 10mg/Nm3The concentration of sulfur dioxide is less than or equal to 50mg/Nm3The concentration of nitrogen oxide is less than or equal to 100mg/Nm3。
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In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a flow chart of a gypsum calcination flue gas treatment process provided by an embodiment of the invention.
Detailed Description
The technical solutions in the embodiments of the present invention are clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention provides a method for treating gypsum calcination flue gas, which comprises the following steps:
a) burning the fuel in a combustion chamber of a gypsum calciner to generate hot flue gas; in the process of burning the fuel, spraying ammonia water and lime powder into the combustion chamber;
b) cooling the hot flue gas, then sending the cooled hot flue gas into a calcining chamber of a gypsum calcining furnace, and calcining gypsum powder in the cooled hot flue gas in the calcining chamber to obtain mixed flue gas;
c) carrying out dry-type electric precipitation on the mixed flue gas to obtain dedusting flue gas and dust; the dust comprises calcined gypsum powder and smoke dust;
d) oxidizing the dedusting flue gas in the presence of an oxidant to obtain oxidized flue gas;
e) carrying out wet desulphurization on the oxidized flue gas to obtain desulfurized nitrate flue gas;
f) and carrying out wet-type electric precipitation on the desulfurized nitrate flue gas to obtain purified flue gas.
In the method provided by the invention, fuel is firstly combusted in a combustion chamber of a gypsum calcining furnace to generate hot flue gas. Wherein the combustion temperature is preferably 800-950 ℃, more preferably 850-900 ℃, and specifically can be 850 ℃, 855 ℃, 860 ℃, 865 ℃, 870 ℃, 875 ℃, 880 ℃, 885 ℃, 890 ℃, 895 ℃ or 900 ℃. In the invention, in order to reduce the content of nitrogen oxides in hot flue gas, ammonia water is sprayed into a combustion chamber in the process of burning the fuel, namely selective non-catalytic reduction denitration (SNCR) is carried out. In the invention, the ammonia water is preferably sprayed into the hot flue gas by a spray gun arranged in the combustion chamber, and the spray gun is asymmetrically distributed along the horizontal direction of the combustion chamber preferably according to the flow characteristics of the flue gasPlacing to ensure that the ammonia water completely covers the hot flue gas; the arrangement position of the spray gun along the vertical direction of the combustion chamber preferably reaches the height that the fuel can be fully combusted to release nitrogen oxides, and the suitable temperature for the ammonia water to carry out the selective non-catalytic reduction reaction is met. In the invention, the concentration of the ammonia water is preferably 10-20 wt%, and specifically 10 wt%, 11 wt%, 12 wt%, 13 wt%, 14 wt%, 15 wt%, 16 wt%, 17 wt%, 18 wt%, 19 wt% or 20 wt%; the ratio of the spraying amount of the ammonia water to the flue gas amount of the combustion chamber is preferably (0.1-0.3) m3H: (6-10) ten thousand Nm3Specifically, it may be (0.2 to 0.3) m3H: (8-9) ten thousand Nm3Or (0.2 to 0.25) m3H: (6-8) ten thousand Nm3. In the invention, in order to reduce the content of sulfur oxides in hot flue gas, in the process of burning the fuel, lime powder is sprayed into a combustion chamber, namely dry desulfurization is carried out; the ratio of the sprayed amount of the lime powder to the amount of flue gas of the combustion chamber is preferably (40-50) kg/h: (6-10) ten thousand Nm3Specifically, (40 to 50) kg/h: (8-9) ten thousand Nm3Or (40-45): (6-8) ten thousand Nm3。
In the method provided by the invention, after hot flue gas is generated, the hot flue gas is cooled to meet the temperature requirement of gypsum powder calcination, then the cooled hot flue gas is conveyed to a calcination chamber of a gypsum calcination furnace, and the gypsum powder is calcined in the calcination chamber by using the cooled hot flue gas. Wherein the temperature of the cooled hot flue gas is preferably 550-650 ℃, and specifically can be 550 ℃, 560 ℃, 570 ℃, 580 ℃, 590 ℃, 600 ℃, 610 ℃, 620 ℃, 630 ℃, 640 ℃ or 650 ℃. In the invention, after calcination, mixed flue gas mixed with calcined gypsum powder is obtained.
In the method provided by the invention, after the mixed flue gas is obtained, dry-type electric precipitation is carried out on the mixed flue gas, so that the dust in the flue gas is collected. The flow speed of the mixed flue gas during dry electric precipitation is preferably controlled to be 0.5-0.6 m/s, and specifically can be 0.5m/s, 0.51m/s, 0.52m/s, 0.53m/s, 0.54m/s, 0.55m/s, 0.56m/s, 0.57m/s, 0.58m/s, 0.59m/s or 0.6 m/s. In the invention, the mixed flue gas is subjected to dry-type electric precipitation to respectively obtain dust and dedusting flue gas, wherein the dust comprises calcined gypsum powder and smoke dust, and the temperature of the dedusting flue gas is preferably 120-160 ℃, more preferably 130-150 ℃, and specifically 130 ℃, 131 ℃, 132 ℃, 133 ℃, 134 ℃, 135 ℃, 136 ℃, 137 ℃, 138 ℃, 139 ℃, 140 ℃, 141 ℃, 142 ℃, 143 ℃, 144 ℃, 145 ℃, 146 ℃, 147 ℃, 148 ℃, 149 ℃ or 150 ℃.
In the method provided by the invention, after the dedusting flue gas is obtained, the dedusting flue gas is oxidized in the presence of an oxidant. Wherein the oxidation is preferably performed in a wet oxidation tower, more preferably in a spray tower, and the oxidizing agent includes, but is not limited to, one or more of sodium chlorite, sodium hypochlorite, ozone, and hydrogen peroxide. In the invention, after oxidation treatment, NO in the flue gas is oxidized into NO which is easily dissolved in water2Can be jointly removed when wet desulphurization is carried out subsequently. In the invention, by adopting the low-temperature oxidation technology for denitration, a catalyst is not needed, the method is suitable for low-temperature flue gas after gypsum powder calcination, and meanwhile, the method can play a certain auxiliary role in subsequent wet desulphurization.
In the method provided by the invention, after the dedusting flue gas is obtained, part of the dedusting flue gas can be returned to the gypsum calcining furnace to be mixed with the hot flue gas, so that the temperature of the hot flue gas is reduced.
In the method provided by the invention, after the dedusting flue gas is obtained, part of the dedusting flue gas can be returned to the gypsum calcining furnace to adjust the air surplus coefficient of the combustion chamber. In one embodiment of the present invention, the air excess coefficient of the combustion chamber is preferably controlled to be 1.5-2.2, and specifically may be 1.5, 1.55, 1.6, 1.65, 1.7, 1.75, 1.8, 1.85, 1.9, 1.95, 2, 2.05, 2.1, 2.15, or 2.2.
In the method provided by the invention, after the oxidation of the dedusting flue gas is finished, the wet desulphurization is carried out on the obtained oxidized flue gas. Wherein, the specific mode of the wet desulphurization is preferably double-alkali desulphurization; the two-alkali desulfurization is preferably carried out in a wet desulfurization tower, more preferably in a spray tower. In the invention, in the operation process of the spray tower, the pH value of the desulfurization absorption liquid entering the spray tower is preferably controlled to be 9-11, and specifically can be 9, 9.5, 10, 10.5 or 11; the pH value of the desulfurization absorption liquid discharged from the tower is preferably controlled to be 6-7.5, and specifically can be 6, 6.5, 7 or 7.5. In the invention, the flue gas outlet end of the spray tower is preferably provided with a demister, and the demister is preferably a baffle demister. In the invention, the purpose of arranging the demister in the spray tower is to pre-remove dust of flue gas at the outlet end of the spray tower. In the invention, after wet desulphurization, the sulfur oxides and nitrogen oxides in the oxidized flue gas are jointly removed to obtain the desulfurized nitrate flue gas.
In the method provided by the invention, after the desulfurized nitrate flue gas is obtained, wet-type electric precipitation is carried out on the desulfurized nitrate flue gas. The wet electric dust remover is used for performing wet electric dust removal, and the flue gas flow velocity of the desulfurized nitrate flue gas in the wet electric dust remover is preferably controlled to be 2-3 m/s, and specifically can be 2m/s, 2.1m/s, 2.2m/s, 2.3m/s, 2.4m/s, 2.5m/s, 2.6m/s, 2.7m/s, 2.8m/s, 2.9m/s or 3 m/s. In one embodiment provided by the invention, the wet electric dust collector adopts a vertical tubular structure and is vertically arranged, the spray device is arranged at the inlet of the dust collector, when the dust collector operates, flue gas and sprayed fog drops are fully combined, and under the action of a direct-current high-voltage electric field, substances such as dust particles, dust-fog mixtures, gypsum particles, aerosol and the like in the flue gas are charged by the electric field, are finally captured by the electric field, are adsorbed on the anode tube and flow out along with a water film on the plate wall of the plate tube. In the invention, after the desulfurized nitrate flue gas is subjected to wet-type electric precipitation, the contents of particulate pollutants and fine fog drops in the flue gas are further reduced, and the purified flue gas is obtained.
According to the invention, aiming at the temperature requirement and the flue gas characteristics of the gypsum calcination process, the reduction method denitration (SNCR) is adopted at the high-temperature section of the flue gas, then the flue gas is cooled and the gypsum calcination is completed, then the dry-method electric precipitation is used for completing the material collection, then the oxidation denitration and the wet-method desulphurization of the low-temperature flue gas are carried out, and finally the wet-method electric precipitation is used for collecting liquid drops and particles in the flue gas, so that the ultralow emission of pollutants in the gypsum calcination flue gas is realized, and the requirement of clean production can be met. The experimental results show that: the treatment method can realize the flue gas pollutants generated in the gypsum calcinationUltra-low emission, the concentration of particulate matter in the treated flue gas is less than or equal to 10mg/Nm3The concentration of sulfur dioxide is less than or equal to 50mg/Nm3The concentration of nitrogen oxide is less than or equal to 100mg/Nm3。
For the sake of clarity, the following examples are given in detail.
Example 1
Treating gypsum calcining flue gas according to the process flow shown in FIG. 1, wherein FIG. 1 is a process flow chart for treating gypsum calcining flue gas provided by the embodiment of the invention, wherein 1 is a blower for blowing air into a combustion chamber of a gypsum calcining furnace; 2, a return fan, which is used for guiding part of the dedusting flue gas to return to the gypsum calcining furnace and participating in the control of the air surplus coefficient of the combustion chamber and the cooling of the hot flue gas; and 3, a draught fan for guiding the dedusting flue gas to the wet oxidation tower.
In this embodiment, a specific flue gas treatment process flow includes: burning the fuel in a combustion chamber of a gypsum calcining furnace, blowing air into the combustion chamber through a blower 1 during the burning, spraying ammonia water into the combustion chamber for SNCR denitration, and spraying lime powder for dry desulfurization; mixing hot flue gas generated by combustion with part of dust removal flue gas generated in a subsequent working section to reduce the temperature of the flue gas, and then sending the cooled flue gas into a calcining chamber of a gypsum calcining furnace to calcine gypsum powder to obtain mixed flue gas mixed with calcined gypsum powder; feeding the obtained mixed flue gas into a dry-type electric dust remover for trapping calcined gypsum powder and smoke dust to obtain a mixture of the calcined gypsum powder and the smoke dust and dust-removing flue gas; one part of the obtained dedusting smoke (low oxygen-containing smoke) flows back through the return fan 2, one part of the returned dedusting smoke flows back to the air blower 1 to be mixed with the air surplus coefficient of the control combustion chamber, and the other part of the returned dedusting smoke flows back to the hot smoke outlet of the combustion chamber to be mixed with the hot smoke, so that the temperature of the smoke is reduced; the rest of the dedusting flue gas enters a wet oxidation tower through a draught fan 3 and is oxidized in the wet oxidation tower; and (3) feeding the oxidized flue gas obtained by oxidation into a wet desulfurization tower to carry out wet combined desulfurization and denitration, and further removing particulate pollutants and fine fog drops from the obtained desulfurization and denitration flue gas in a wet electric dust remover to obtain purified flue gas.
In the flue gas treatment process flow provided by the embodiment, the temperature of the combustion chamber is controlled to be 850-900 ℃, and the air excess coefficient of the combustion chamber is controlled to be 1.75-2; the flue gas amount of the combustion chamber is 6-10 ten thousand Nm3(ii) a The concentration of the ammonia water is 10-20 wt%, and the spraying amount of the ammonia water is 0.1-0.3 m3H; the spraying amount of the lime powder is about 50 kg/h; the temperature of the cooled flue gas is 600 ℃.
In the flue gas treatment process flow provided by this embodiment, the operating conditions of the dry-type electric dust remover are as follows: controlling the flow rate of flue gas to be 0.5-0.6 m/s; the temperature of the dedusting flue gas is 130-150 ℃.
In the flue gas treatment process flow provided by this embodiment, the wet oxidation tower is a spray tower, and the oxidizing agent is sodium chlorite; the operating conditions of the wet oxidation tower are as follows: the spraying amount of the sodium chlorite is controlled to meet the flue gas index at the outlet of the wet oxidation tower.
In the process flow for treating flue gas provided by this embodiment, the wet desulfurization tower is a spray tower with a baffle demister at the flue gas outlet end, and the desulfurization mode is dual-alkali desulfurization; the operating conditions of the wet desulphurization tower are as follows: controlling the pH of the liquid discharged from the tower to be 6-7, and controlling the pH of the liquid entering the tower to be 10-11.
In the flue gas treatment process flow provided by the embodiment, the wet electric dust remover adopts a vertical tubular structure and is vertically arranged, and a spray device is arranged at the inlet of the dust remover; the wet electric dust remover has the following operating conditions: the flow velocity of the flue gas is controlled to be 2-3 m/s.
In the flue gas treatment process flow provided by this embodiment, the flue gas pollutant concentration conditions of each section are as follows:
1) the outlet of the gypsum calcining furnace is mixed with mixed flue gas for calcining gypsum powder: the concentration of the particles is less than 400g/m3The concentration of nitrogen oxides is less than 150mg/m3The concentration of sulfur dioxide is less than 200mg/m3；
2) Dust removal flue gas at the outlet of the dry electric precipitator: the concentration of the particles is less than 30mg/m3Nitrogen oxide concentration is less than 150mg/m3The concentration of sulfur dioxide is less than 200mg/m3；
3) Oxidation flue gas at the outlet of the wet oxidation tower: particulate matterThe concentration is less than 20mg/m3The concentration of nitrogen oxides is less than 100mg/m3The concentration of sulfur dioxide is less than 200mg/m3；
4) Desulfurization nitre flue gas at the outlet of the wet desulfurization tower: the concentration of the particles is less than 20mg/m3The concentration of nitrogen oxides is less than 100mg/m3The concentration of sulfur dioxide is less than 50mg/m3；
5) Purifying flue gas at the outlet of the wet electric precipitator: the concentration of the particulate matters is less than 10mg/m3, and the concentration of the nitrogen oxides is less than 100mg/m3The concentration of sulfur dioxide is less than 50mg/m3。
Example 2
The gypsum calcination flue gas is treated according to the process flow shown in fig. 1, and the specific flue gas treatment process flow comprises the following steps: burning the fuel in a combustion chamber of a gypsum calcining furnace, blowing air into the combustion chamber through a blower 1 during the burning, spraying ammonia water into the combustion chamber for SNCR denitration, and spraying lime powder for dry desulfurization; mixing hot flue gas generated by combustion with part of dust removal flue gas generated in a subsequent working section to reduce the temperature of the flue gas, and then sending the cooled flue gas into a calcining chamber of a gypsum calcining furnace to calcine gypsum powder to obtain mixed flue gas mixed with calcined gypsum powder; feeding the obtained mixed flue gas into a dry-type electric dust remover for trapping calcined gypsum powder and smoke dust to obtain a mixture of the calcined gypsum powder and the smoke dust and dust-removing flue gas; one part of the obtained dedusting smoke (low oxygen-containing smoke) flows back through the return fan 2, one part of the returned dedusting smoke flows back to the air blower 1 to be mixed with the air surplus coefficient of the control combustion chamber, and the other part of the returned dedusting smoke flows back to the hot smoke outlet of the combustion chamber to be mixed with the hot smoke, so that the temperature of the smoke is reduced; the rest of the dedusting flue gas enters a wet oxidation tower through a draught fan 3 and is oxidized in the wet oxidation tower; and (3) feeding the oxidized flue gas obtained by oxidation into a wet desulfurization tower to carry out wet combined desulfurization and denitration, and further removing particulate pollutants and fine fog drops from the obtained desulfurization and denitration flue gas in a wet electric dust remover to obtain purified flue gas.
In the flue gas treatment process flow provided by the embodiment, the temperature of the combustion chamber is controlled to be 850-900 ℃, and the air surplus coefficient of the combustion chamber is controlled to be 1.7-2; flue gas amount of combustion chamberIs 8 to 9 ten thousand Nm3(ii) a The concentration of the ammonia water is 10-20 wt%, and the spraying amount of the ammonia water is 0.2-0.3 m3H; the spraying amount of the lime powder is about 40-50 kg/h; the temperature of the cooled flue gas is 600 ℃.
In the flue gas treatment process flow provided by this embodiment, the operating conditions of the dry-type electric dust remover are as follows: controlling the flow rate of flue gas to be 0.5-0.6 m/s; the temperature of the dedusting flue gas is 130-150 ℃.
In the flue gas treatment process flow provided by this embodiment, the wet oxidation tower is a spray tower, and the oxidizing agent is sodium chlorite; the operating conditions of the wet oxidation tower are as follows: and controlling the spraying amount of the oxidant to meet the flue gas index at the outlet of the wet oxidation tower.
In the process flow for treating flue gas provided by this embodiment, the wet desulfurization tower is a spray tower with a baffle demister at the flue gas outlet end, and the desulfurization mode is dual-alkali desulfurization; the operating conditions of the wet desulphurization tower are as follows: controlling the pH of the liquid discharged from the tower to be 6.5-7.5, and controlling the pH of the liquid entering the tower to be 10-11.
In the flue gas treatment process flow provided by the embodiment, the wet electric dust remover adopts a vertical tubular structure and is vertically arranged, and a spray device is arranged at the inlet of the dust remover; the wet electric dust remover has the following operating conditions: the flow velocity of the flue gas is controlled to be 2-3 m/s.
In the flue gas treatment process flow provided by this embodiment, the flue gas pollutant concentration conditions of each section are as follows:
1) the outlet of the gypsum calcining furnace is mixed with mixed flue gas for calcining gypsum powder: the concentration of the particles is less than 400g/m3The concentration of nitrogen oxides is less than 150mg/m3The concentration of sulfur dioxide is less than 200mg/m3；
2) Dust removal flue gas at the outlet of the dry electric precipitator: the concentration of the particles is less than 30mg/m3Nitrogen oxide concentration is less than 150mg/m3The concentration of sulfur dioxide is less than 200mg/m3；
3) Oxidation flue gas at the outlet of the wet oxidation tower: the concentration of the particles is less than 20mg/m3The concentration of nitrogen oxides is less than 100mg/m3The concentration of sulfur dioxide is less than 200mg/m3；
4) Desulfurization nitre flue gas at the outlet of the wet desulfurization tower: the concentration of the particles is less than 20mg/m3The concentration of nitrogen oxides is less than 100mg/m3The concentration of sulfur dioxide is less than 50mg/m3；
5) Purifying flue gas at the outlet of the wet electric precipitator: the concentration of the particulate matters is less than 10mg/m3, and the concentration of the nitrogen oxides is less than 100mg/m3The concentration of sulfur dioxide is less than 50mg/m3。
Example 3
The gypsum calcination flue gas is treated according to the process flow shown in fig. 1, and the specific flue gas treatment process flow comprises the following steps: burning the fuel in a combustion chamber of a gypsum calcining furnace, blowing air into the combustion chamber through a blower 1 during the burning, spraying ammonia water into the combustion chamber for SNCR denitration, and spraying lime powder for dry desulfurization; mixing hot flue gas generated by combustion with part of dust removal flue gas generated in a subsequent working section to reduce the temperature of the flue gas, and then sending the cooled flue gas into a calcining chamber of a gypsum calcining furnace to calcine gypsum powder to obtain mixed flue gas mixed with calcined gypsum powder; feeding the obtained mixed flue gas into a dry-type electric dust remover for trapping calcined gypsum powder and smoke dust to obtain a mixture of the calcined gypsum powder and the smoke dust and dust-removing flue gas; one part of the obtained dedusting smoke (low oxygen-containing smoke) flows back through the return fan 2, one part of the returned dedusting smoke flows back to the air blower 1 to be mixed with the air surplus coefficient of the control combustion chamber, and the other part of the returned dedusting smoke flows back to the hot smoke outlet of the combustion chamber to be mixed with the hot smoke, so that the temperature of the smoke is reduced; the rest of the dedusting flue gas enters a wet oxidation tower through a draught fan 3 and is oxidized in the wet oxidation tower; and (3) feeding the oxidized flue gas obtained by oxidation into a wet desulfurization tower to carry out wet combined desulfurization and denitration, and further removing particulate pollutants and fine fog drops from the obtained desulfurization and denitration flue gas in a wet electric dust remover to obtain purified flue gas.
In the flue gas treatment process flow provided by the embodiment, the temperature of the combustion chamber is controlled to be 850-900 ℃, and the air excess coefficient of the combustion chamber is controlled to be 1.75-2; the flue gas amount of the combustion chamber is 6-8 ten thousand Nm3(ii) a The concentration of the ammonia water is 10-20 wt%, and the spraying amount of the ammonia water is 0.2-0.25 m3H; the spraying amount of the lime powder is about 40-45 kg/h; temperature reductionThe temperature of the flue gas is 600 ℃.
In the flue gas treatment process flow provided by this embodiment, the operating conditions of the dry-type electric dust remover are as follows: controlling the flow rate of flue gas to be 0.5-0.6 m/s; the temperature of the dedusting flue gas is 130-150 ℃.
In the flue gas treatment process flow provided by this embodiment, the wet oxidation tower is a spray tower, and the oxidizing agent is sodium chlorite; the operating conditions of the wet oxidation tower are as follows: and controlling the spraying amount of the oxidant to meet the flue gas index at the outlet of the wet oxidation tower.
In the process flow for treating flue gas provided by this embodiment, the wet desulfurization tower is a spray tower with a baffle demister at the flue gas outlet end, and the desulfurization mode is dual-alkali desulfurization; the operating conditions of the wet desulphurization tower are as follows: controlling the pH of the liquid discharged from the tower to be 6.5-7.5, and controlling the pH of the liquid entering the tower to be 9-11.
In the flue gas treatment process flow provided by the embodiment, the wet electric dust remover adopts a vertical tubular structure and is vertically arranged, and a spray device is arranged at the inlet of the dust remover; the wet electric dust remover has the following operating conditions: the flow velocity of the flue gas is controlled to be 2-3 m/s.
In the flue gas treatment process flow provided by this embodiment, the flue gas pollutant concentration conditions of each section are as follows:
1) the outlet of the gypsum calcining furnace is mixed with mixed flue gas for calcining gypsum powder: the concentration of the particles is less than 400g/m3The concentration of nitrogen oxides is less than 150mg/m3The concentration of sulfur dioxide is less than 200mg/m3；
2) Dust removal flue gas at the outlet of the dry electric precipitator: the concentration of the particles is less than 30mg/m3Nitrogen oxide concentration is less than 150mg/m3The concentration of sulfur dioxide is less than 200mg/m3；
3) Oxidation flue gas at the outlet of the wet oxidation tower: the concentration of the particles is less than 20mg/m3The concentration of nitrogen oxides is less than 100mg/m3The concentration of sulfur dioxide is less than 200mg/m3；
4) Desulfurization nitre flue gas at the outlet of the wet desulfurization tower: the concentration of the particles is less than 20mg/m3The concentration of nitrogen oxides is less than 100mg/m3Sulfur dioxide concentration is less50mg/m3；
5) Purifying flue gas at the outlet of the wet electric precipitator: the concentration of the particulate matters is less than 10mg/m3, and the concentration of the nitrogen oxides is less than 100mg/m3The concentration of sulfur dioxide is less than 50mg/m3。
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (3)
1. A method for treating gypsum calcination flue gas comprises the following steps:
burning the fuel in a combustion chamber of a gypsum calcining furnace, blowing air into the combustion chamber through a blower during the burning, spraying ammonia water into the combustion chamber for SNCR denitration, and spraying lime powder for dry desulfurization; mixing hot flue gas generated by combustion with part of dust removal flue gas generated in a subsequent working section to reduce the temperature of the flue gas, and then sending the cooled flue gas into a calcining chamber of a gypsum calcining furnace to calcine gypsum powder to obtain mixed flue gas mixed with calcined gypsum powder; feeding the obtained mixed flue gas into a dry-type electric dust remover for trapping calcined gypsum powder and smoke dust to obtain a mixture of the calcined gypsum powder and the smoke dust and dust-removing flue gas; one part of the obtained dedusting flue gas flows back through a return fan, one part of the returned dedusting flue gas flows back to a blower and is mixed with an air surplus coefficient of a control combustion chamber, and the other part of the returned dedusting flue gas flows back to a hot flue gas outlet of the combustion chamber and is mixed with the hot flue gas, so that the temperature of the flue gas is reduced; the rest of the dedusting flue gas enters a wet oxidation tower through a draught fan and is oxidized in the wet oxidation tower; the oxidized flue gas obtained by oxidation enters a wet desulfurization tower to carry out wet combined desulfurization and denitration, and the obtained desulfurization and denitration flue gas further removes particulate pollutants and fine fog drops in a wet electric dust remover to obtain purified flue gas;
in the flue gas treatment process, the temperature of the combustion chamber is controlled to be 850-900 ℃, and the air surplus coefficient of the combustion chamber is controlled to be 1.75-2; carrying out dry distillation on the flue gas in the combustion chamber, wherein the flue gas amount in the combustion chamber is 6-10 ten thousand Nm; the concentration of the ammonia water is 10-20 wt%, and the spraying amount of the ammonia water is 0.1-0.3 m/h; the spraying amount of the lime powder is about 50 kg/h; the temperature of the cooled flue gas is 600 ℃;
in the flue gas treatment process, the operation conditions of the dry-type electric dust remover are as follows: controlling the flow rate of flue gas to be 0.5-0.6 m/s; the temperature of the dedusting flue gas is 130-150 ℃;
the wet oxidation tower is a spray tower; in the flue gas treatment process, sodium chlorite is used as an oxidant; the operating conditions of the wet oxidation tower are as follows: controlling the spraying amount of sodium chlorite to meet the flue gas index at the outlet of the wet oxidation tower;
the wet desulphurization tower is a spray tower of which the flue gas outlet end is provided with a baffle plate demister; in the flue gas treatment process, the desulfurization mode is dual-alkali desulfurization; the operating conditions of the wet desulphurization tower are as follows: controlling the pH of the liquid discharged from the tower to be 6-7, and controlling the pH of the liquid entering the tower to be 10-11;
the wet electric dust collector adopts a vertical tubular structure and is vertically arranged, and a spray device is arranged at the inlet of the dust collector; in the flue gas treatment process, the operation conditions of the wet electric dust remover are as follows: controlling the flow rate of flue gas to be 2-3 m/s;
in the flue gas treatment process, the concentration conditions of the flue gas pollutants in each section are as follows:
1) the outlet of the gypsum calcining furnace is mixed with mixed flue gas for calcining gypsum powder: carrying out dry-mass transformation on the obtained grain particles;
2) dust removal flue gas at the outlet of the dry electric precipitator: carrying out double-cropping lotus according to the specific sequence, wherein the concentration of the particulate matters is less than 30mg/m, the concentration of the nitric oxides is less than 150mg/m, and the concentration of the sulfur dioxide is less than 200 mg/m;
3) oxidation flue gas at the outlet of the wet oxidation tower: carrying out dry-mass transformation on the obtained dry-mass transformed plant, wherein the particulate matter concentration is less than 20mg/m, the nitrogen oxide concentration is less than 100mg/m and the sulfur dioxide concentration is less than 200 mg/m;
4) desulfurization nitre flue gas at the outlet of the wet desulfurization tower: carrying out double-cropping lotus according to the specific sequence, wherein the particulate matter concentration is less than 20mg/m, the nitrogen oxide concentration is less than 100mg/m, and the sulfur dioxide concentration is less than 50 mg/m;
5) purifying flue gas at the outlet of the wet electric precipitator: and (3) carrying out heavy labor according to the condition that the concentration of the particulate matters is less than 10mg/m, carrying out heavy labor according to the condition that the concentration of the nitrogen oxides is less than 100mg/m, and carrying out heavy labor according to the condition that the concentration of the sulfur dioxide is less than 50 mg/m.
2. A method for treating gypsum calcination flue gas comprises the following steps:
burning the fuel in a combustion chamber of a gypsum calcining furnace, blowing air into the combustion chamber through a blower during the burning, spraying ammonia water into the combustion chamber for SNCR denitration, and spraying lime powder for dry desulfurization; mixing hot flue gas generated by combustion with part of dust removal flue gas generated in a subsequent working section to reduce the temperature of the flue gas, and then sending the cooled flue gas into a calcining chamber of a gypsum calcining furnace to calcine gypsum powder to obtain mixed flue gas mixed with calcined gypsum powder; feeding the obtained mixed flue gas into a dry-type electric dust remover for trapping calcined gypsum powder and smoke dust to obtain a mixture of the calcined gypsum powder and the smoke dust and dust-removing flue gas; one part of the obtained dedusting flue gas flows back through a return fan, one part of the returned dedusting flue gas flows back to a blower and is mixed with an air surplus coefficient of a control combustion chamber, and the other part of the returned dedusting flue gas flows back to a hot flue gas outlet of the combustion chamber and is mixed with the hot flue gas, so that the temperature of the flue gas is reduced; the rest of the dedusting flue gas enters a wet oxidation tower through a draught fan and is oxidized in the wet oxidation tower; the oxidized flue gas obtained by oxidation enters a wet desulfurization tower to carry out wet combined desulfurization and denitration, and the obtained desulfurization and denitration flue gas further removes particulate pollutants and fine fog drops in a wet electric dust remover to obtain purified flue gas;
in the flue gas treatment process, the temperature of the combustion chamber is controlled to be 850-900 ℃, and the air surplus coefficient of the combustion chamber is controlled to be 1.7-2; carrying out dry distillation on the flue gas in the combustion chamber, wherein the flue gas amount of the combustion chamber is 8-9 ten thousand Nm; the concentration of the ammonia water is 10-20 wt%, and the spraying amount of the ammonia water is 0.2-0.3 m/h; the spraying amount of the lime powder is 40-50 kg/h; the temperature of the cooled flue gas is 600 ℃;
in the flue gas treatment process, the operation conditions of the dry-type electric dust remover are as follows: controlling the flow rate of flue gas to be 0.5-0.6 m/s; the temperature of the dedusting flue gas is 130-150 ℃;
the wet oxidation tower is a spray tower; in the flue gas treatment process, sodium chlorite is used as an oxidant; the operating conditions of the wet oxidation tower are as follows: controlling the spraying amount of the oxidant to meet the flue gas index at the outlet of the wet oxidation tower;
the wet desulphurization tower is a spray tower of which the flue gas outlet end is provided with a baffle plate demister; in the flue gas treatment process, the desulfurization mode is dual-alkali desulfurization; the operating conditions of the wet desulphurization tower are as follows: controlling the pH of the liquid discharged from the tower to be 6.5-7.5, and controlling the pH of the liquid entering the tower to be 10-11;
the wet electric dust collector adopts a vertical tubular structure and is vertically arranged, and a spray device is arranged at the inlet of the dust collector; in the flue gas treatment process, the operation conditions of the wet electric dust remover are as follows: controlling the flow rate of flue gas to be 2-3 m/s;
in the flue gas treatment process, the concentration conditions of the flue gas pollutants in each section are as follows:
1) the outlet of the gypsum calcining furnace is mixed with mixed flue gas for calcining gypsum powder: carrying out dry-mass transformation on the obtained grain particles;
2) dust removal flue gas at the outlet of the dry electric precipitator: carrying out double-cropping lotus according to the specific sequence, wherein the concentration of the particulate matters is less than 30mg/m, the concentration of the nitric oxides is less than 150mg/m, and the concentration of the sulfur dioxide is less than 200 mg/m;
3) oxidation flue gas at the outlet of the wet oxidation tower: carrying out dry-mass transformation on the obtained dry-mass transformed plant, wherein the particulate matter concentration is less than 20mg/m, the nitrogen oxide concentration is less than 100mg/m and the sulfur dioxide concentration is less than 200 mg/m;
4) desulfurization nitre flue gas at the outlet of the wet desulfurization tower: carrying out double-cropping lotus according to the specific sequence, wherein the particulate matter concentration is less than 20mg/m, the nitrogen oxide concentration is less than 100mg/m, and the sulfur dioxide concentration is less than 50 mg/m;
5) purifying flue gas at the outlet of the wet electric precipitator: and (3) carrying out heavy labor according to the condition that the concentration of the particulate matters is less than 10mg/m, carrying out heavy labor according to the condition that the concentration of the nitrogen oxides is less than 100mg/m, and carrying out heavy labor according to the condition that the concentration of the sulfur dioxide is less than 50 mg/m.
3. A method for treating gypsum calcination flue gas comprises the following steps:
burning the fuel in a combustion chamber of a gypsum calcining furnace, blowing air into the combustion chamber through a blower during the burning, spraying ammonia water into the combustion chamber for SNCR denitration, and spraying lime powder for dry desulfurization; mixing hot flue gas generated by combustion with part of dust removal flue gas generated in a subsequent working section to reduce the temperature of the flue gas, and then sending the cooled flue gas into a calcining chamber of a gypsum calcining furnace to calcine gypsum powder to obtain mixed flue gas mixed with calcined gypsum powder; feeding the obtained mixed flue gas into a dry-type electric dust remover for trapping calcined gypsum powder and smoke dust to obtain a mixture of the calcined gypsum powder and the smoke dust and dust-removing flue gas; one part of the obtained dedusting flue gas flows back through a return fan, one part of the returned dedusting flue gas flows back to a blower and is mixed with an air surplus coefficient of a control combustion chamber, and the other part of the returned dedusting flue gas flows back to a hot flue gas outlet of the combustion chamber and is mixed with the hot flue gas, so that the temperature of the flue gas is reduced; the rest of the dedusting flue gas enters a wet oxidation tower through a draught fan and is oxidized in the wet oxidation tower; the oxidized flue gas obtained by oxidation enters a wet desulfurization tower to carry out wet combined desulfurization and denitration, and the obtained desulfurization and denitration flue gas further removes particulate pollutants and fine fog drops in a wet electric dust remover to obtain purified flue gas;
in the flue gas treatment process, the temperature of the combustion chamber is controlled to be 850-900 ℃, and the air surplus coefficient of the combustion chamber is controlled to be 1.75-2; carrying out dry distillation on the flue gas in the combustion chamber, wherein the flue gas amount in the combustion chamber is 6-8 ten thousand Nm; the concentration of the ammonia water is 10-20 wt%, and the spraying amount of the ammonia water is 0.2-0.25 m/h; the spraying amount of the lime powder is 40-45 kg/h; the temperature of the cooled flue gas is 600 ℃;
in the flue gas treatment process, the operation conditions of the dry-type electric dust remover are as follows: controlling the flow rate of flue gas to be 0.5-0.6 m/s; the temperature of the dedusting flue gas is 130-150 ℃;
the wet oxidation tower is a spray tower; in the flue gas treatment process, sodium chlorite is used as an oxidant; the operating conditions of the wet oxidation tower are as follows: controlling the spraying amount of the oxidant to meet the flue gas index at the outlet of the wet oxidation tower;
the wet desulphurization tower is a spray tower of which the flue gas outlet end is provided with a baffle plate demister; in the flue gas treatment process, the desulfurization mode is dual-alkali desulfurization; the operating conditions of the wet desulphurization tower are as follows: controlling the pH of the liquid discharged from the tower to be 6.5-7.5, and controlling the pH of the liquid entering the tower to be 9-11;
the wet electric dust collector adopts a vertical tubular structure and is vertically arranged, and a spray device is arranged at the inlet of the dust collector; in the flue gas treatment process, the operation conditions of the wet electric dust remover are as follows: controlling the flow rate of flue gas to be 2-3 m/s;
in the flue gas treatment process, the concentration conditions of the flue gas pollutants in each section are as follows:
1) the outlet of the gypsum calcining furnace is mixed with mixed flue gas for calcining gypsum powder: carrying out dry-mass transformation on the obtained grain particles;
2) dust removal flue gas at the outlet of the dry electric precipitator: carrying out double-cropping lotus according to the specific sequence, wherein the concentration of the particulate matters is less than 30mg/m, the concentration of the nitric oxides is less than 150mg/m, and the concentration of the sulfur dioxide is less than 200 mg/m;
3) oxidation flue gas at the outlet of the wet oxidation tower: carrying out dry-mass transformation on the obtained dry-mass transformed plant, wherein the particulate matter concentration is less than 20mg/m, the nitrogen oxide concentration is less than 100mg/m and the sulfur dioxide concentration is less than 200 mg/m;
4) desulfurization nitre flue gas at the outlet of the wet desulfurization tower: carrying out double-cropping lotus according to the specific sequence, wherein the particulate matter concentration is less than 20mg/m, the nitrogen oxide concentration is less than 100mg/m, and the sulfur dioxide concentration is less than 50 mg/m;
5) purifying flue gas at the outlet of the wet electric precipitator: and (3) carrying out heavy labor according to the condition that the concentration of the particulate matters is less than 10mg/m, carrying out heavy labor according to the condition that the concentration of the nitrogen oxides is less than 100mg/m, and carrying out heavy labor according to the condition that the concentration of the sulfur dioxide is less than 50 mg/m.
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