CN110559816B - Flue gas desulfurization tower and flue gas dedusting, desulfurization and wastewater treatment process - Google Patents
Flue gas desulfurization tower and flue gas dedusting, desulfurization and wastewater treatment process Download PDFInfo
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- CN110559816B CN110559816B CN201810569009.2A CN201810569009A CN110559816B CN 110559816 B CN110559816 B CN 110559816B CN 201810569009 A CN201810569009 A CN 201810569009A CN 110559816 B CN110559816 B CN 110559816B
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- flue gas
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- clear liquid
- pipeline
- tower
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- 239000003546 flue gas Substances 0.000 title claims abstract description 268
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 264
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 99
- 230000023556 desulfurization Effects 0.000 title claims abstract description 99
- 238000000034 method Methods 0.000 title claims abstract description 49
- 230000008569 process Effects 0.000 title claims abstract description 44
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 201
- 239000000428 dust Substances 0.000 claims abstract description 96
- 238000005189 flocculation Methods 0.000 claims abstract description 92
- 230000016615 flocculation Effects 0.000 claims abstract description 92
- 230000003647 oxidation Effects 0.000 claims abstract description 88
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 88
- 238000005507 spraying Methods 0.000 claims abstract description 67
- 238000001816 cooling Methods 0.000 claims abstract description 51
- 238000005192 partition Methods 0.000 claims abstract description 46
- 238000010791 quenching Methods 0.000 claims abstract description 32
- 230000000171 quenching effect Effects 0.000 claims abstract description 32
- 238000009826 distribution Methods 0.000 claims abstract description 13
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 8
- 239000002002 slurry Substances 0.000 claims description 74
- 239000007789 gas Substances 0.000 claims description 48
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 44
- 230000001590 oxidative effect Effects 0.000 claims description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 43
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- 230000001105 regulatory effect Effects 0.000 claims description 23
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- 150000003839 salts Chemical class 0.000 claims description 17
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 15
- 230000009471 action Effects 0.000 claims description 12
- 230000001276 controlling effect Effects 0.000 claims description 11
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- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 9
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
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- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 6
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- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 5
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 2
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- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 2
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Abstract
The invention discloses a flue gas desulfurization tower and a flue gas dedusting, desulfurizing and wastewater treatment process. A flue gas desulfurization tower comprises a flue gas discharge area, a demisting area, a tower tray area, a spraying area, a quenching and cooling area and a wastewater treatment area from top to bottom in sequence; the wastewater treatment area is divided into an oxidation flocculation area and a circulating clear liquid area by a vertical partition plate I, and the top of the circulating clear liquid area completely separates the circulating clear liquid area from the oxidation flocculation area and the spraying area by a partition plate II; the vertical clapboard I is provided with a filter medium; inside flue gas pipeline II extended to the oxidation flocculation district, inside flue gas pipeline II in oxidation flocculation district horizontal distribution a plurality of groups flue gas branch pipe in proper order from bottom to top. The invention carries out flue gas dust removal, desulfurization, desalination and wastewater treatment in one tower, greatly reduces the occupied area, and reduces the cost required by the construction and the reconstruction of the device and the operation cost of the device.
Description
Technical Field
The invention belongs to the field of industrial waste gas purification, and relates to a flue gas desulfurization tower and a flue gas dedusting, desulfurizing and wastewater treatment process.
Background
The flue gas of the coal-fired boiler and the regenerated flue gas of the catalytic cracking catalyst contain sulfur dioxide and dust, the sulfur dioxide and the dust are main component dust of atmospheric pollutants, the sulfur dioxide is a main reason for forming acid rain, and the dust with smaller particle size is one of the main causes of haze formation.
Environmental pollution is increasingly serious, haze events are frequent, the national degree of attention on environmental protection is also higher and higher, and a series of laws and regulations, national standards and management methods for environmental protection are provided in recent years. GB 13223 Specification of 2011 emission Standard of atmospheric pollutants for thermal power plants: flue gas dust of coal-fired boiler not more than 30mg/Nm3SO of flue gas of newly-built coal-fired boiler2≯100mg/Nm3(ii) a The fume dust of coal-fired boiler in key areas is not more than 20mg/Nm3，SO2≯50mg/Nm3. Complete implementation of working schemes for ultralow emission and energy conservation modification of coal-fired power plants (environmental protection [2015 ]]164) the ultra-low emission indexes of the flue gas of the coal-fired power plant are as follows: flue gas dust not more than 10mg/Nm3， SO2≯25mg/Nm3. GB 31570 2015 emission Standard for Industrial pollutants for Petroleum refining stipulates: regenerated flue gas particulate matters of the catalytic cracking catalyst are not more than 50mg/Nm3，SO2≯100mg/Nm3(ii) a Particulate matter in key areas is not more than 30mg/Nm3， SO2≯50mg/Nm3。
The purification technology of the coal-fired boiler flue gas and the catalytic cracking catalyst regeneration flue gas sulfur dioxide is divided into a dry method, a semi-dry method and a wet method. The wet desulphurization has the advantages of high desulphurization rate, reliable device operation, simple operation and the like, so the existing flue gas desulphurization technology of various countries in the world mainly takes wet desulphurization as the main technology. The traditional wet desulphurization technology mainly comprises a limestone-gypsum method, double-alkali desulphurization, sodium-alkali desulphurization, ammonia desulphurization and the like, most of the technologies adopt a single tower or double towers for flue gas desulphurization, the purified flue gas is discharged from a tower top chimney, and the desulphurization wastewater is extracted from the tower bottom to be oxidized and discharged after reaching the standard or returned to the desulphurization tower for recycling after being regenerated. The flue gas desulfurization technology mainly adopts countercurrent spray, alkaline slurry is sprayed from the upper part of a desulfurization tower, and is free to settle under the action of gravity to be in countercurrent contact with flue gas to realize desulfurization reaction, but the diameter of sprayed liquid drops is relatively large, the contact area of single liquid drop and the flue gas is small, so that in order to improve the desulfurization efficiency, the number of times of circulating spray of the slurry needs to be increased, the liquid drops are in contact with the flue gas for many times to improve the absorption effect of the liquid drops on sulfur dioxide, the flow of a slurry circulating pump at the bottom of the tower is very large, the power of a motor is also very large, the power consumption of the slurry circulating pump is very large, and the operation cost is high.
The particle size of dust in the flue gas is small, most of dust particles are 0.1-200 mu m, dust removal equipment such as a common gravity dust collector, an inertial dust collector and a cyclone separator cannot meet the requirement of flue gas dust removal easily, and the existing flue gas dust removal technology mainly comprises a cloth bag type dust removal technology, an electrostatic dust removal technology and a wet dust removal technology. Because the flue gas contains moisture, dust absorbs moisture and is bonded on a filter bag of the cloth bag type dust collector to block the pores of the filter bag, so that the filter bag needs to be cleaned or replaced frequently, and the application of the cloth bag type dust collector is greatly limited; the main disadvantages of the electrostatic dust collector are that the manufacturing cost is high, the requirements of installation, maintenance and management are strict, high-voltage power transformation and rectification control equipment is required, the power consumption is high, and the occupied area is large; the wet dust removal technology mainly removes dust carried in flue gas through spray water, and liquid drops with smaller particle sizes are still discharged out of a chimney along with the flue gas after being combined with the dust.
The desulfurization wastewater treatment processes disclosed in CN201110153423.3, CN201310338193.7 and CN201310421183.X are all provided with a flocculation tank and an oxidation tank, the flocculation tank and the oxidation tank are both provided with a stirrer, and slurry is conveyed by a pump. The dust removal and desulfurization wastewater treatment process disclosed by CN201310338193.7 and CN201310421183.X adopts a hydrocyclone to carry out solid-liquid separation. The desulfurization wastewater treatment process has the advantages of longer flow, more equipment and higher energy consumption.
Because the pollution emission indexes established by the state are more and more strict, enterprises with coal-fired boilers and oil refineries with catalytic units need to continuously modify the coal-fired boilers and the catalytic cracking units so as to meet the emission standard of flue gas. Most coal-fired boilers and catalytic cracking devices are built according to old standards before, and the smoke needs to be subjected to further deep dust removal and desulfurization during construction, so that enough construction land for smoke dust removal and desulfurization modification is not reserved during construction, and the smoke dust removal and desulfurization devices are required to be newly built or old devices are required to be modified in the existing limited area. The wet desulphurization technology comprises a flue gas desulphurization unit, a desulphurization waste water oxidation treatment unit or a regeneration unit, the flow is long, the number of equipment is large, the occupied area is large, the construction, the upgrading and the reconstruction of a dust removal desulphurization device are seriously restricted, and the partial catalytic device and the coal-fired boiler cannot be upgraded and reconstructed due to the lack of enough space, so that the flue gas emission index cannot meet the current national standard and is forced to be shut down or destroyed and reconstructed. Therefore, the development of flue gas desulfurization technology with short flow, less equipment and less floor space is urgently needed.
In addition, because the wet desulphurization device adopts the circulating liquid containing a large amount of suspended solids and soluble salts as a working medium for flue gas quenching cooling and desulphurization, the circulating liquid is contacted with high-temperature flue gas to realize the flue gas quenching cooling process, a large amount of water is vaporized, and the soluble salts and the suspended solids enter the flue gas along with the vaporized water, so that the flue gas at the outlet of the wet desulphurization device contains more soluble salts (mainly sulfate and sulfite), the soluble salts form ultrafine particles after dehydration, the ultrafine particles can provide sufficient condensation nuclei for the formation of haze, and the wet desulphurization is also one of the causes of the haze.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides the flue gas desulfurization tower and the flue gas dedusting, desulfurizing and wastewater treatment process.
The flue gas desulfurization tower comprises a flue gas discharge area, a demisting area, a tower tray area, a spraying area, a quenching and cooling area and a wastewater treatment area from top to bottom in sequence; the central part of the wastewater treatment area is divided into an oxidation flocculation area and a circulating clear liquid area through a vertical partition plate I, wherein the oxidation flocculation area is communicated with the spraying area, and the top of the circulating clear liquid area is completely separated from the oxidation flocculation area and the spraying area through a partition plate II.
The partition plate I is provided with at least one opening, preferably 1-20 openings, more preferably 1-4 openings, and the area of the opening is 10% -90% of that of the partition plate I, preferably 50% -70%; a filter medium is fixed on the opening of the clapboard I; the filter medium is of a net structure, the mesh size is 0.1-1000 mu m, preferably 5-100 mu m, and the filter medium can be made of natural fibers, synthetic fibers, glass fibers or metal wires.
The two ends of the baffle plate II are respectively connected with the baffle plate I and the tower wall of the circulating clear liquid area, and the included angle of the joint of the baffle plate I and the baffle plate II is generally 45-165 degrees, preferably 120-150 degrees. The partition plates I and II are sealed with the tower wall, so that gas and liquid short circuits at two sides of the partition plates are avoided.
The flue gas discharge area and the demisting area are preferably connected through conical reducing, and the tower diameter ratio of the demisting area to the flue gas discharge area is 1.2-5; the tower disc area and the spraying area are preferably connected through an inverted cone-shaped reducing area, and a wastewater treatment area is arranged below the spraying area; the tower diameter ratio of the tower tray area to the spraying area is 1.2-3.
And the top of the smoke discharge area is provided with a smoke outlet for discharging purified smoke.
The demisting zone is provided with demisting equipment for removing liquid drops carried by the flue gas, and the demisting equipment can be one or more of a cyclone demister, a wet electrostatic demister, a wire mesh demister or a baffling demister.
The tower tray area can be provided with one or more layers of tower trays, and the number of the tower trays is preferably 2-6; the tower tray can be one type of tower tray or various types of combined tower trays, comprises a float valve tower tray, a sieve tray, a guide sieve tray, a tongue fixing tower tray, a tongue floating tower tray or a three-dimensional mass transfer tower tray and the like, is used for gas-liquid full contact reinforced mass transfer to realize deep desulfurization of flue gas, captures micro dust particles between 0.1 mu m and 5 mu m in the flue gas to realize deep dust removal of the flue gas, and captures a large amount of micro fog drops carried by the flue gas to reduce the separation load of a demisting area.
And a liquid distributor is arranged between the tower tray area and the demisting area, and is connected with a circulating clear liquid pipeline I and used for uniformly distributing circulating clear liquid on the tower tray.
One or more layers of spraying pipelines are arranged at the upper part of the spraying area, and when the plurality of layers of spraying pipelines are arranged, the distance between the spraying pipelines is 0.5-5 m, and the preferable distance is 1-2.5 m; the spraying pipeline is connected with a circulating clear liquid pipeline II and is provided with a plurality of atomizing nozzles; the spraying area is used for atomizing the circulating clear liquid, and the atomized small liquid drops are in countercurrent contact with the flue gas to remove dust and sulfur dioxide carried in the flue gas.
A plurality of large-caliber atomizing nozzles with upward or downward openings are axially arranged at the upper part of the rapid cooling and cooling zone, each large-caliber atomizing nozzle is connected with a clean water branch pipe, and the clean water branch pipe is connected with a clean water main pipe; the ratio of the pipe diameter of an inlet joint of the large-diameter atomizing nozzle to the tower diameter of the quenching and cooling area is 0.005-0.1, and preferably 0.01-0.06; the spraying angle of the large-caliber atomizing nozzle is 60-150 degrees, and the preferred angle is 120-150 degrees; the sprayed water mist is in a solid conical shape, and the diameter of the conical bottom surface is larger than the tower diameter of the quenching and cooling area; preferably at least comprises a pair of large-caliber atomizing nozzles with opposite openings (one opening is downward, the other opening is upward), and more preferably 2-3 pairs; two conical surfaces sprayed out by each pair of large-diameter atomizing nozzles with opposite openings mutually collide to form a plane covering the whole tower diameter, the plane comprehensively and effectively intercepts flue gas, the rapid cooling and the temperature reduction of the flue gas are realized, and dust and sulfur dioxide carried in the flue gas are removed. Each clean water branch pipe can be connected with 1 large-caliber atomizing nozzle or 2 large-caliber atomizing nozzles with opposite opening directions; the pipe diameter of an inlet joint of the large-caliber atomizing nozzle can be generally DN 20-200; and the lower part of the quenching and cooling area is provided with a flue gas inlet I which is used for connecting a flue gas pipeline I.
One side of the oxidation flocculation area, which is close to the tower wall, is respectively connected with an alkaline solution pipeline I, a flocculating agent pipeline and a liquid level meter I; the alkaline solution pipeline I is provided with a flow regulating valve for adding an alkaline solution into the desulfurization wastewater to regulate the pH value of the desulfurization wastewater; the flocculant pipeline is used for injecting a flocculant into the desulfurization wastewater, so that small-particle dust in the desulfurization wastewater is coagulated into large particles.
The bottom of the oxidation flocculation area is connected with a flue gas pipeline II and an outer discharging slurry pipeline; the flue gas pipeline II extends to the inside of the oxidation flocculation zone and is parallel to the partition plate I, a plurality of groups of flue gas branch pipes, preferably 2-4 groups of flue gas branch pipes, are horizontally distributed in sequence from bottom to top on the flue gas pipeline II in the oxidation flocculation zone, and the flue gas branch pipes are communicated with the flue gas pipeline II; each group of flue gas branch pipes consists of 2-8 flue gas branch pipes, each flue gas branch pipe is arc-shaped, and each group of flue gas branch pipes are uniformly distributed in the horizontal direction and have the same rotating direction; the spraying direction of the flue gas from the flue gas branch pipe is the tangential direction of an arc, the flue gas is sprayed at a high speed to push the slurry to rotate, the slurry in the oxidation flocculation area is stirred, the materials in the oxidation flocculation area are uniformly mixed, and dust particles on the filter medium are washed off; the external slurry discharge pipeline is used for discharging the slurry after oxidation and flocculation to a subsequent treatment unit, and a flow regulating valve and a pH meter are arranged on the external slurry discharge pipeline; the flow regulating valve regulates the flow of the discharged slurry according to a signal fed back by the liquid level meter I and is used for controlling the liquid level of the liquefaction flocculation area; the pH meter is used for measuring the pH value of the discharged slurry and feeding back a signal to the flow regulating valve on the alkaline solution pipeline I through the controller.
One side of the circulating clear liquid zone, which is close to the tower wall, is connected with a fresh water pipeline, an alkaline solution pipeline II, an oxidizing gas pipeline and a liquid level meter II; the fresh water pipeline is provided with a flow regulating valve which is used for regulating the flow of fresh water according to a signal fed back by the liquid level meter II and controlling the liquid level of the circulating clear liquid area; the alkaline solution pipeline II is provided with a flow regulating valve for regulating the flow of the alkaline solution filled into the circulating clear liquid area; the oxidizing gas pipeline is connected with the fan, extends to one side of the partition plate I of the circulating clear liquid zone and is connected with the oxidizing gas distribution pipe; the oxidizing gas distribution pipe is provided with a plurality of nozzles, the nozzles are opposite to the filter medium on the partition plate I, the oxidizing gas is sprayed out from the nozzles and penetrates through the filter medium to blow up dust particles on the filter medium in the oxidation flocculation area, the blown-up dust and the oxidizing gas are taken away by the rotating slurry, the dust and the flocculating agent are coagulated into large particles to be deposited at the bottom of the oxidation flocculation area under the action of gravity, and the oxidizing gas entering the oxidation flocculation area oxidizes sulfite in the slurry into sulfate so that the COD of the desulfurization wastewater reaches the standard.
The tower wall at the top of the circulating clear liquid area is provided with an air vent for ensuring the stable pressure of the circulating clear liquid area and avoiding the damage to the filter medium caused by overlarge pressure fluctuation.
The bottom of the circulating clear liquid zone is connected with a clear liquid leading-out pipeline, the leading-out pipeline is divided into two paths, one path of pipeline is connected with an external clear liquid discharging pipeline, the other path of pipeline is connected with a circulating clear liquid pump, a pH meter is arranged on the pipeline, and the circulating clear liquid pump is connected with a circulating clear liquid pipeline I and a circulating clear liquid pipeline II through a cooler; the pH meter is used for measuring the pH value of the circulating clear liquid and feeding back a measurement signal to the regulating valve of the alkaline solution pipeline II through the controller.
The invention relates to a process for dedusting and desulfurizing flue gas and treating wastewater, which comprises the following steps:
(1) flue gas enters a flue gas desulfurization tower in two paths, one path of flue gas enters from the lower part of a quenching and cooling area of the flue gas desulfurization tower through a flue gas pipeline I, the other path of flue gas enters from the bottom of an oxidation and flocculation area of the flue gas desulfurization tower through a flue gas pipeline II after being pressurized and passes through slurry in the oxidation and flocculation area, the two paths of flue gas are converged and then contact with clean water atomized by the quenching and cooling area to carry out quenching and cooling, the quenched and cooled flue gas enters a spraying area and is in countercurrent contact with circulating clear liquid in the spraying area to remove most of dust and sulfur dioxide carried in the flue gas, the flue gas passing through the spraying area enters a tower panel area, deep dedusting and desulfurization are carried out on the tower panel area and the circulating clear liquid, and the purified flue gas is demisted by a demisting area and then is discharged from a flue gas discharge area;
(2) the desulfurization slurry absorbing the dust and the sulfur dioxide enters an oxidation flocculation area, and is fully mixed with oxidizing gas, a flocculating agent and an alkaline solution under the stirring action of the flue gas entering through a flue gas pipeline II, sulfite in the desulfurization slurry is oxidized into sulfate, small particle dust in the desulfurization slurry is flocculated into large particles, and meanwhile, the flue gas with a certain temperature enables the moisture in the desulfurization slurry to be continuously volatilized, and the salt concentration is gradually increased;
(3) the desulfurization slurry flows through a filter medium on a partition plate I to realize solid-liquid separation under the action of liquid level difference on two sides of the partition plate I, dust particles in the desulfurization slurry are filtered and left in an oxidation flocculation area, clear liquid enters a circulating clear liquid area, and the slurry after oxidation flocculation is led out from the bottom of the oxidation flocculation area and enters a subsequent treatment unit through an external discharge pipeline;
(4) oxidizing gas enters from the circulating clear liquid zone, is sprayed out from a nozzle of the oxidizing gas distribution pipe and penetrates through the filter medium, dust particles on the filter medium of the oxidation flocculation zone are blown up, the blown-up dust and the oxidizing gas are taken away by the rotating slurry, the dust and a flocculating agent are aggregated into large particles under the action of gravity and are deposited at the bottom of the oxidation flocculation zone, and sulfite in the slurry is oxidized into sulfate by the oxidizing gas entering the oxidation flocculation zone, so that the COD of the desulfurization wastewater reaches the standard;
(5) the clear liquid entering the circulating clear liquid zone after being filtered by the filter medium is mixed with fresh water and alkaline solution in the circulating clear liquid zone and then is led out from the bottom of the circulating clear liquid zone, a small amount of clear liquid is directly discharged to reduce the salt concentration of the circulating clear liquid, the rest clear liquid enters the cooler after being pressurized by the circulating clear liquid pump, one part of the clear liquid cooled by the cooler enters the spraying area, is atomized by the atomizing nozzle and then is in countercurrent contact with the flue gas to remove dust and sulfur, the other part of the clear liquid flows through the liquid distributor and enters the tower disc area, the deep desulfurization of flue gas is realized with the abundant contact of flue gas intensive mass transfer effect on the tray to catch the small dust particle between 0.1 mu m ~5 mu m in the flue gas, realize the degree of depth dust removal of flue gas, a large amount of small fog drops that the flue gas carried through the spray area also are caught by the clear liquid on the tray, have reduced the separation load that removes the fog district.
In the process, the flue gas in the step (1) is coal-fired boiler flue gas, coal-fired power plant flue gas, catalytic cracking catalyst regeneration flue gas, process heating furnace flue gas, coking flue gas or steel sintering flue gas and the like. The ratio of the amount of the flue gas entering the flue gas pipeline I to the amount of the flue gas entering the flue gas pipeline II is 20-500; the ratio of clean water to flue gas in the quenching and cooling zone is 0.05-2.5L/Nm3Preferably 0.1 to 1.5L/Nm3(ii) a The ratio of the circulating clear liquid to the flue gas in the spraying area is 5-50L/Nm3The preferred proportion is 8-25L/Nm3And the ratio of the circulating clear liquid to the flue gas in the tower tray area is 3-15L/Nm3。
In the process, the content of soluble salt (total soluble solid) in the clean water is less than or equal to 30g/L, preferably less than or equal to 5 g/L; the clean water is one or more selected from fresh water, desalted water, softened water, deoxidized water or distilled water, and the fresh water is selected from tap water, river water, sea water or well water. Clean water enters the quenching and cooling area through a clean water pipeline.
In the process, the alkaline solution in the steps (2) and (5) is selected from one or more of sodium hydroxide solution, calcium hydroxide solution, magnesium hydroxide solution, sodium carbonate solution, sodium sulfite solution, sodium citrate solution, limestone slurry, ammonia water or seawater and the like.
In the process of the invention, the oxidizing gas in the steps (2) and (4) is one or more of air, oxygen, ozone and the like, and preferably the oxidizing gas is air.
In the process, the flow of the oxidizing gas in the steps (2) and (4) is adjusted according to the Chemical Oxygen Demand (COD) of the slurry after flocculation concentration, and the COD control index is not more than 60 mg/L.
In the process, the flocculating agent in the steps (2) and (4) is one or more of aluminum sulfate, alum, sodium aluminate, ferric trichloride, ferrous sulfate, ferric sulfate, polyaluminum chloride, polyaluminum sulfate, polyaluminum phosphate, polyferric chloride, polyferric sulfate, polymeric ferric phosphate, polymeric ferric chloride, polymeric aluminum chloride, polysilicate iron, polysilicate ferric sulfate, polyaluminum sulfate silicate, polymeric ferric aluminum sulfate chloride, polymeric polyferric silicon flocculating agent, aluminum-iron copolymerization composite flocculating agent, polysilicate flocculating agent, polyacrylamide flocculating agent and the like, and the adding amount of the flocculating agent is 0.05-2 kg/m3。
In the process, the pH value of the slurry after the oxidation flocculation in the step (3) is controlled to be 7-9, the pH online detector is positioned on a slurry external discharge pipeline, and the pH value of the desulfurized slurry is controlled by adjusting an adjusting valve on an alkaline solution pipeline I.
In the process, the liquid level difference between two sides of the partition plate I in the step (3) is 0.5-6 m, and the liquid level of the oxidation flocculation area is higher than that of the circulating clear liquid area.
In the process, the liquid level height of the oxidation flocculation area in the step (3) is controlled by an adjusting valve on an external slurry discharge pipeline.
In the process, the liquid level height of the circulating clear liquid area in the step (3) is controlled by an adjusting valve on a fresh water pipeline.
In the process, the pH value of the circulating clear liquid area in the steps (3) to (5) is controlled to be 6-11, the preferable control range of the pH value is 7-8, the pH online detector is positioned on an inlet pipeline of a tower bottom circulating pump, and the pH value of the circulating clear liquid is controlled by adjusting an adjusting valve on an alkaline solution pipeline II.
In the process, the discharged slurry in the step (3) and the discharged clear liquid in the step (5) enter a subsequent treatment unit, can be used for preparing or producing products such as gypsum, sodium sulfite, sodium bisulfite, magnesium sulfite, magnesium sulfate, magnesium oxide, sodium sulfate, ammonium bisulfate and the like, and can also be discharged after being filtered to reach the standard.
Compared with the prior art, the invention has the advantages that:
1. the invention arranges a wastewater treatment area at the lower part of the desulfurizing tower, divides the wastewater treatment area into an oxidation flocculation area and a circulating clear liquid area through two clapboards, and realizes the oxidation, flocculation and concentration of the desulfurizing wastewater in the oxidation flocculation area; the vertical clapboard in the center of the wastewater treatment area is provided with a filter medium, and the filtration operation of the desulfurization slurry is realized by using the liquid level difference at the two sides of the vertical clapboard as a driving force. The circulating clear liquid obtained by filtering is used as a circulating medium for dust removal and desulfurization, and because the circulating clear liquid does not contain dust or has low dust content, compared with the prior art that slurry containing dust is used as the circulating medium for dust removal and desulfurization, the process has high dust removal efficiency. The invention divides the inlet flue gas into two paths, wherein the high-temperature flue gas entering from the bottom of the oxidation flocculation area is sprayed out from the arc-shaped flue gas branch pipe along the tangential direction to push the dust removal desulfurization waste liquid to rotate, so that the materials in the oxidation flocculation area are fully mixed and contacted, the oxidation flocculation reaction is facilitated, the dust and sulfur-containing oxides in the flue gas are absorbed to a certain extent, meanwhile, the waste heat of the high-temperature flue gas is fully utilized, the moisture in the dust removal desulfurization waste water is greatly vaporized, the primary concentration of the desulfurization waste water is realized in the oxidation flocculation area, and the energy consumption of subsequent units is reduced. Meanwhile, the oxidizing gas is introduced from the circulating clear liquid zone instead of directly entering the oxidation flocculation zone, and the oxidizing gas is used for washing the filter medium, so that washing equipment is omitted. The invention saves conventional stirring equipment and filtering equipment, does not need to consume additional energy in the wastewater treatment process, and greatly reduces the device investment and the operation cost.
2. The large-caliber atomizing nozzles with opposite openings are arranged in the rapid cooling and cooling area, two conical surfaces sprayed by each pair of large-caliber atomizing nozzles with opposite openings mutually collide to form a plane covering the whole tower diameter, the plane comprehensively and effectively intercepts flue gas, rapid cooling and cooling of the flue gas are realized, and dust and sulfur dioxide carried in the flue gas are removed.
3. According to the invention, clean water with low soluble salt (total soluble solid) content is adopted in the quenching and cooling zone to replace circulating liquid containing a large amount of suspended matters and soluble salts as a high-temperature flue gas quenching and cooling medium, the content of soluble salts in vaporized water vapor in the flue gas quenching and cooling process is very low, the content of soluble salts in discharged flue gas is greatly reduced, and the generation amount of haze is favorably reduced.
4. According to the invention, the inverted cone-shaped reducing is arranged between the tray area and the spraying area, so that the gas velocity of the tray area is favorably reduced, the gas-liquid mass transfer effect is enhanced, the dust removal efficiency and the desulfurization efficiency of flue gas in the tray area are improved, and entrainment is reduced, so that the load of the demisting area is reduced; the smoke discharging area and the demisting area are provided with the cone-shaped reducing areas, so that the flow speed of smoke is improved, the higher the gas speed of the smoke is, the higher the lifting height of the smoke after the smoke leaves the smoke discharging area is, the more the smoke is favorably diffused, and smoke plumes are shorter.
5. The invention completes flue gas dust removal, flue gas desulfurization and wastewater treatment in one tower, realizes triple functions of deep flue gas dust removal, desulfurization and standard-reaching wastewater COD discharge, has short process flow and remarkably reduces the cost required by device construction and transformation due to the cooperative cooperation of all functional areas.
Drawings
FIG. 1 is a schematic view of a flue gas desulfurization tower according to the present invention.
FIG. 2 is a schematic view of the structure of the separator in the direction of A.
FIG. 3 is a schematic view of a direction B of a wastewater treatment zone according to the present invention.
FIG. 4 is a schematic view of the process of the present invention.
In the figure: 1-a flue gas discharge zone; 2-conical reducing; 3-a demisting area; 4-tower disc area; 5-inverted cone-shaped reducing; 6-spraying area; 6-1-circulating clear liquid line II; 7-a wastewater treatment zone; 8-an oxidative flocculation zone; 8-1-level gauge I; 8-2-alkaline solution line I; 8-3-flocculant line; 8-4-an efflux slurry line; 8-5-flue gas pipeline II; 9-circulating clear liquid area; 9-1-level gauge II; 9-2-fresh water line; 9-3-alkaline solution line II; 9-4-oxidizing gas line; 9-5-clear liquid outlet line; 9-6-an efflux supernatant line; 10-a flue gas inlet; 11-a demister; 12-a liquid distributor; 12-1-recycle serum line I; 13-trays; 14-a spray line; 15-an atomizing nozzle; 16-a vent; 17-flue gas branch pipe; an 18-oxidizing gas distribution pipe; 19-separator II; 20-a separator I; 21-a filter medium; 22-a sealing strip; 23-a fastening screw; 24-a fan; 25-a cooler; 26-circulating clear liquid pump; 27-a quenching cooling zone; 27-1 clean water main; 27-2-flue gas line I; 28-large caliber atomizing nozzle; 29-clean water branch pipes; 30-a supercharger.
Detailed Description
The present invention will be described in detail below with reference to the drawings and examples.
The flue gas desulfurization tower comprises a flue gas discharge area 1, a demisting area 3, a tower tray area 4, a spraying area 6, a quenching and cooling area 27 and a wastewater treatment area 7 from top to bottom in sequence; waste water treatment district 7 central authorities divide into oxidation flocculation district 8 and circulation clear solution district 9 through a vertical baffle I20, wherein oxidation flocculation district 8 and spraying district 6 intercommunication, circulation clear solution district 9 top is separated circulation clear solution district 9 and oxidation flocculation district 8 and spraying district 6 completely through baffle II 19.
The partition plate I20 is provided with at least one opening, preferably 1-20 openings, more preferably 1-4 openings, and the area of the opening is 10% -90% of the area of the partition plate I20, preferably 50% -70%; a filter medium 21 is fixed on the opening of the clapboard I20; the filter medium 21 is of a net structure, the mesh size is 0.1-1000 mu m, preferably 5-100 mu m, and the filter medium can be made of natural fibers, synthetic fibers, glass fibers or metal wires.
Two ends of the partition plate II 19 are respectively connected with the partition plate I20 and the tower wall of the circulating clear liquid zone 9, and the included angle of the joint of the partition plate I20 and the partition plate II 19 is generally 45-165 degrees, preferably 120-150 degrees. The partition plates I20 and II 19 are sealed with the tower wall, so that gas and liquid short circuits at two sides of the partition plates are avoided.
The flue gas discharge area 1 and the demisting area 3 are preferably connected through a cone-shaped reducing area 2, and the tower diameter ratio of the demisting area 3 to the flue gas discharge area 1 is 1.2-5; the tower disc area 4 is preferably connected with the spraying area 6 through an inverted cone-shaped reducing area 5, a quenching and cooling area 27 is arranged below the spraying area 6, and a wastewater treatment area 7 is arranged below the quenching and cooling area 27; the tower tray area 4 and the spray area 6 have the tower diameter ratio of 1.2-3.
The top of the smoke discharge area 1 is provided with a smoke outlet for discharging purified smoke.
Demisting zone 3 set up demisting equipment for detach the liquid drop that the flue gas carried, demisting equipment can be for one or several kinds among whirl defroster, wet-type electrostatic demister, silk screen defroster or baffling formula defroster etc. preferably adopt CN201621043983.8 the defroster.
One or more layers of tower trays 13 can be arranged in the tower tray area 4, and the number of the tower tray layers is preferably 2-6; the tower tray can be one type of tower tray or various types of combined tower trays, comprises a float valve tower tray, a sieve tray, a guide sieve tray, a tongue fixing tower tray, a tongue floating tower tray or a three-dimensional mass transfer tower tray and the like, is used for gas-liquid full contact reinforced mass transfer to realize deep desulfurization of flue gas, captures micro dust particles between 0.1 mu m and 5 mu m in the flue gas to realize deep dust removal of the flue gas, and captures a large amount of micro fog drops carried by the flue gas to reduce the separation load of a demisting area 3.
And a liquid distributor 12 is arranged between the tray area 4 and the demisting area 3, and the liquid distributor 12 is connected with a circulating clear liquid pipeline I12-1 and is used for uniformly distributing circulating clear liquid on a tray 13.
One or more layers of spraying pipelines 14 are arranged at the upper part of the spraying area 6, and when the plurality of layers of spraying pipelines 14 are arranged, the distance between the spraying pipelines 14 is 0.5-5 m, and the preferable distance is 1-2.5 m; the spraying pipeline 14 is connected with the circulating clear liquid pipeline II 6-1, and a plurality of atomizing nozzles 15 are arranged on the spraying pipeline 14; the spraying area 6 is used for atomizing the circulating clear liquid, and the atomized small liquid drops are in countercurrent contact with the flue gas to remove dust and sulfur dioxide carried in the flue gas.
A plurality of large-caliber atomizing nozzles 28 with upward or downward openings are axially arranged at the upper part of the rapid cooling and cooling zone 27, each large-caliber atomizing nozzle 28 is connected with a clean water branch pipe 29, and the clean water branch pipe 29 is connected with a clean water main pipe 27-1; the ratio of the pipe diameter of the inlet joint of the large-diameter atomizing nozzle 28 to the tower diameter of the quenching and cooling area 27 is 0.005-0.1, preferably 0.01-0.06; the spraying angle of the large-diameter atomizing nozzle 28 is 60-150 degrees, and the preferred angle is 120-150 degrees; the sprayed water mist is in a solid conical shape, and the diameter of the conical bottom surface is larger than the tower diameter of the quenching and cooling area 27; preferably at least one pair of large-diameter atomizing nozzles 28 with opposite openings (one opening is downward, the other opening is upward), more preferably 2-3 pairs; two conical surfaces sprayed by each pair of large-diameter atomizing nozzles 28 with opposite openings mutually collide to form a plane covering the whole tower diameter, the plane comprehensively and effectively intercepts flue gas, the quenching and cooling of the flue gas are realized, and dust and sulfur dioxide carried in the flue gas are removed. Each clean water branch pipe 29 can be connected with 1 large-caliber atomizing nozzle 28 or 2 large-caliber atomizing nozzles 28 with opposite opening directions; the pipe diameter of the inlet joint of the large-diameter atomizing nozzle 28 can be generally DN 20-200; the lower part of the rapid cooling and cooling area 27 is provided with a flue gas inlet I10 which is used for connecting a flue gas pipeline I27-2.
One side of the oxidation flocculation area 8, which is close to the tower wall, is respectively connected with an alkaline solution pipeline I8-2, a flocculant pipeline 8-3 and a liquid level meter I8-1; the alkaline solution pipeline I8-2 is provided with a flow regulating valve for adding an alkaline solution into the desulfurization wastewater to regulate the pH value of the desulfurization wastewater; and the flocculant pipeline 8-3 is used for injecting a flocculant into the desulfurization wastewater so as to coagulate small-particle dust in the desulfurization wastewater into large particles.
The bottom of the oxidation flocculation area 8 is connected with a flue gas pipeline II 8-5 and an outer discharge slurry pipeline 8-4; the flue gas pipeline II 8-5 extends to the inside of the oxidation flocculation zone 8 and is parallel to the partition plate I20, the flue gas pipeline II 8-5 in the oxidation flocculation zone 8 is sequentially and horizontally distributed with a plurality of groups of flue gas branch pipes 17 from bottom to top, preferably 2-4 groups, and the flue gas branch pipes 17 are communicated with the flue gas pipeline II 8-5; each group of flue gas branch pipes 17 consists of 2-8 flue gas branch pipes 17, each flue gas branch pipe 17 is arc-shaped, and each group of flue gas branch pipes 17 are uniformly distributed in the horizontal direction and have the same rotating direction; the spraying direction of the flue gas from the flue gas branch pipe 17 is the tangential direction of an arc, the flue gas is sprayed at a high speed to push the slurry to rotate, the slurry in the oxidation flocculation area 8 is stirred, the materials in the oxidation flocculation area are uniformly mixed, and dust particles on the filter medium 21 are washed off; the external slurry discharge pipeline 8-4 is used for discharging oxidized and flocculated slurry to a subsequent treatment unit, and a flow regulating valve and a pH meter are arranged on the external slurry discharge pipeline 8-4; the flow regulating valve regulates the flow of the discharged slurry according to a signal fed back by the liquid level meter I8-1 and is used for controlling the liquid level of the liquefaction flocculation area; the pH meter is used for measuring the pH value of the discharged slurry and feeding back a signal to the flow regulating valve on the alkaline solution pipeline I8-2 through the controller.
One side of the circulating clear liquid zone 9, which is close to the tower wall, is connected with a fresh water pipeline 9-2, an alkaline solution pipeline II9-3, an oxidizing gas pipeline 9-4 and a liquid level meter II 9-1; a flow regulating valve is arranged on the fresh water pipeline 9-2, and the flow of the fresh water is regulated according to a signal fed back by the liquid level meter II9-1, so as to control the liquid level of the circulating clear water area 9; the alkaline solution pipeline II9-3 is provided with a flow regulating valve for regulating the flow of the alkaline solution filled into the circulating clear liquid zone 9; the oxidizing gas pipeline 9-4 is connected with a fan 24, extends to one side of the partition plate I20 of the circulating clear liquid zone 9 and is connected with an oxidizing gas distribution pipe 18; the oxidizing gas distribution pipe 18 is provided with a plurality of nozzles, the nozzles are opposite to the filter medium 21 on the partition plate I20, the oxidizing gas is sprayed out from the nozzles and penetrates through the filter medium 21, dust particles on the filter medium 21 of the oxidation flocculation area 8 are blown up, the blown-up dust and the oxidizing gas are taken away by the rotating slurry, the dust and a flocculating agent are coagulated into large particles under the action of gravity and are deposited at the bottom of the oxidation flocculation area 8, and the oxidizing gas entering the oxidation flocculation area 8 oxidizes sulfite in the slurry into sulfate so as to ensure that the COD of the desulfurization wastewater reaches the standard.
And the tower wall at the top of the circulating clear liquid area 9 is provided with an air vent 16 for ensuring the stable pressure of the circulating clear liquid area 9 and avoiding the damage to the filter medium 21 caused by overlarge pressure fluctuation.
The bottom of the circulating clear liquid zone 9 is connected with a clear liquid outlet pipeline 9-5, the outlet pipeline is divided into two paths, one path of pipeline is connected with an externally-discharged clear liquid pipeline 9-6, the other path of pipeline is connected with a circulating clear liquid pump 26, a pH meter is arranged on the pipeline, and the circulating clear liquid pump 26 is connected with a circulating clear liquid pipeline I12-1 and a circulating clear liquid pipeline II 6-1 through a cooler 25; the pH meter is used for measuring the pH value of the circulating clear liquid and feeding back a measurement signal to the regulating valve of the alkaline solution pipeline II9-3 through the controller.
Example 1
The utility model provides a flue gas desulfurization tower, from top to bottom is flue gas discharge district 1, defogging district 3, tower tray district 4, spray district 6, rapid cooling district 27 and waste water treatment district 7 in proper order, and flue gas discharge district 1 links to each other through the cone form reducing 2 with defogging district 3, and defogging district 3 below is tower tray district 4, and tower tray district 4 links to each other through the inverted cone form reducing 5 with spray district 6, and spray district 6 below is rapid cooling district 27, and rapid cooling district 27 below is waste water treatment district 7.
A demister 11 described in CN201621043983.8 is arranged in the demisting zone 3, a liquid distributor 12 is arranged below the demisting zone 3, a tray zone 4 is arranged below the liquid distributor 12, the tray zone 4 is provided with 4 layers of trays in total, and sieve trays are selected; the spraying area 6 is provided with 3 layers of spraying pipelines 14, the distance between the spraying pipelines 14 is 2m, and the atomizing nozzles 15 are uniformly arranged on the spraying pipelines 14; two pairs of large-caliber atomizing nozzles 28 with opposite openings (one opening is downward and the other opening is upward) are axially arranged at the upper part of the rapid cooling and cooling zone 27, the large-caliber atomizing nozzles 28 are connected with clean water branch pipes 29, and the clean water branch pipes 29 are connected with a clean water main pipe 27-1.
Waste water treatment district 7 central authorities divide into oxidation flocculation district 8 and circulation clear solution district 9 through a vertical baffle I20, and wherein oxidation flocculation district 8 and spraying district 6 intercommunication, circulation clear solution district 9 top is separated circulation clear solution district 9 and oxidation flocculation district 8 and spraying district 6 completely through baffle II 19, and baffle I20 links to each other through welding mode with baffle II 19, and baffle I20, baffle II 19 link to each other through welding mode between with the tower wall. An opening is formed in the partition plate I20, a metal net 21 with the aperture of 100 mu m is fixed in the opening area on one side of the oxidation flocculation area 8, and the metal net 21 is fixed on the partition plate I20 through a sealing strip 22 and a fastening screw 23; a flue gas pipeline II 8-5 is arranged at the bottom of the oxidation flocculation area 8, 5 groups of flue gas branch pipes 17 are arranged on the part of the flue gas pipeline II 8-5 extending to the oxidation flocculation area 8, each group of flue gas branch pipes 17 are uniformly distributed in the horizontal direction and have the same rotating direction, each group of flue gas branch pipes 17 consists of 4 flue gas branch pipes 17, and each flue gas branch pipe 17 is arc-shaped; an oxidizing gas pipeline 9-4 is arranged at one side of the circulating clear liquid zone 9 close to the tower wall, and the oxidizing gas pipeline 9-4 extends to one side of a partition plate I20 of the circulating clear liquid zone 9 and is connected with an oxidizing gas distribution pipe 18; the oxidizing gas distribution pipe 18 is provided with a plurality of nozzles which are opposite to the filter medium 21 on the partition plate I20; the tower wall at the upper part of the circulating clear liquid zone 9 is provided with an air vent 16.
The process for dedusting, desulfurizing and treating waste water of flue gas is to treat flue gas containing dust and sulfur dioxide as regenerated catalytic cracking catalyst, but not limited to this kind of flue gas. The process for flue gas dust removal, desulfurization and wastewater treatment of the embodiment specifically comprises the following steps:
(1) the flue gas enters the flue gas desulfurization tower in two paths, one path enters from the lower part of a spraying area 6 of the flue gas desulfurization tower through a flue gas pipeline I27-2, the other path enters from the bottom of an oxidation flocculation area 8 of the flue gas desulfurization tower through a flue gas pipeline II 8-5 after being pressurized by a supercharger 30 and passes through the slurry in the oxidation flocculation area 8, wherein the flue gas flow ratio of the flue gas pipeline I27-2 to the flue gas pipeline II 8-5 is 18, the two paths of flue gas are converged and then contacted with clean water atomized by the quenching and cooling area 27 for quenching and cooling, the quenched and cooled flue gas enters the spraying area 6 and is in countercurrent contact with circulating clear liquid of the spraying area 6 to remove most of dust and sulfur dioxide carried in the flue gas, the flue gas passing through the spraying area 6 enters the tower panel area 4, deep dedusting and desulfurization are carried out on the tower tray area 4 and the circulating clear liquid, and the purified flue gas is demisted by the demisting area 3 and then is discharged from the flue gas discharge area 1;
(2) enabling the desulfurization slurry absorbing dust and sulfur dioxide to enter an oxidation flocculation area 8, controlling the pH value of desulfurization wastewater in the oxidation flocculation area 8 to be 7.5-8 by adjusting the flow of a sodium hydroxide solution (32 w%), fully mixing the desulfurization slurry with air, a polysilicic acid flocculant and a sodium hydroxide solution under the stirring action of flue gas entering through a flue gas pipeline II 8-5, oxidizing sulfite in the desulfurization slurry into sulfate, flocculating small particle dust in the desulfurization slurry into large particles, and enabling the moisture in the desulfurization slurry to be volatilized continuously by the flue gas with a certain temperature and gradually increasing the salt concentration;
(3) controlling the liquid level height of an oxidation flocculation area 8 by adjusting the flow of discharged slurry 8-6, and controlling the liquid level height of a circulating clear liquid area 9 by adjusting the flow of fresh water 9-2, so that the liquid level difference between the liquid level of the oxidation flocculation area 8 and the liquid level difference between the circulating clear liquid area 9 is kept at 1.0-2.0 m, the desulfurization slurry flows through a metal net 21 on a partition plate I20 under the action of the liquid level difference between two sides of a partition plate I20 to realize solid-liquid separation, dust particles in the desulfurization slurry are filtered and left in the oxidation flocculation area 8, clear liquid enters the circulating clear liquid area 9, and the slurry after oxidation flocculation is led out from the bottom of the oxidation flocculation area 8 and enters a subsequent treatment unit through a discharge pipeline;
(4) air from a fan 24 enters from the circulating clear liquid zone 9, is sprayed out from a nozzle of the oxidizing gas distribution pipe 18 and penetrates through the metal mesh 21, dust particles on the metal mesh 21 of the oxidation flocculation zone 8 are blown up, the blown-up dust and the oxidizing gas are taken away by the rotating slurry, the dust and the flocculating agent are aggregated into large particles under the action of gravity and deposited at the bottom of the oxidation flocculation zone, and the oxidizing gas entering the oxidation flocculation zone 8 oxidizes sulfite in the slurry into sulfate so as to ensure that the COD of the desulfurization wastewater reaches the standard;
(5) controlling the pH value of the desulfurization wastewater in the circulating clear liquid zone 9 to be 7.0-7.5 by adjusting the flow of a sodium hydroxide solution (32 wt%) entering the circulating clear liquid zone 9, filtering the mixture by a metal mesh 21, mixing the clear liquid entering the circulating clear liquid zone 9 with fresh water and a sodium hydroxide solution in the circulating clear liquid zone 9, leading out the mixture from the bottom of the circulating clear liquid zone 9, directly discharging a small amount of clear liquid to reduce the sodium sulfate content of the circulating clear liquid, pressurizing the rest clear liquid by a circulating clear liquid pump 26, then feeding the pressurized clear liquid into a cooler 25 to cool to 35 ℃, feeding a part of the clear liquid cooled by the cooler 25 into a spray zone 6, atomizing the atomized clear liquid by an atomizing nozzle 15 to be in countercurrent contact with the flue gas to remove dust and sulfur, feeding the other part of the clear liquid into a tray tower plate 4 through a liquid distributor 12, fully contacting with the flue gas on a tray 13 to strengthen the mass transfer effect to realize deep desulfurization of the flue gas, and catching micro dust particles between 0.1 mu m and 5 mu m in the flue gas, the deep dust removal of the flue gas is realized, a large amount of micro fog drops carried by the flue gas through the spraying area 6 are also captured by clear liquid on the tower tray 13, and the separation load of the demisting area 3 is reduced.
Example 2
The smoke volume of a certain enterprise is 220000Nm3The temperature of the flue gas is 145 ℃, the pressure is 4.5kPa, wherein the SO2The concentration is 1200mg/Nm3The dust concentration was 260mg/Nm3By adopting the flue gas desulfurization tower, the flow of clean water in a quenching and cooling area is 80 m3H is used as the reference value. SO in the externally discharged flue gas2The content is measured by a German Degraph flue gas analyzer (model Testo-350), the dust content is measured according to GB/T16157-2The concentration was 11.6mg/Nm3The dust content was 9.3mg/Nm3The content of soluble salt is 1.5 mg/Nm3。
Example 3
The valve on the clean water pipeline entering the quenching and cooling area 27 is closed, and the flow of the clean water is adjusted to 0m3The rest of the same procedure as in example 2, the temperature of the flue gas discharged into the chimney was 51 ℃ and SO2The content is 14.8mg/Nm3The dust content was 21.3mg/Nm3The content of soluble salt is 9.4 mg/Nm3。
Claims (26)
1. A flue gas desulfurization tower is characterized in that: the device comprises a flue gas discharge area, a demisting area, a tower tray area, a spraying area, a quenching and cooling area and a wastewater treatment area from top to bottom in sequence; the top of the smoke discharge area is provided with a smoke outlet; the demisting area is provided with demisting equipment; one or more layers of trays are arranged in the tray area; the center of the wastewater treatment area is divided into an oxidation flocculation area and a circulating clear liquid area through a vertical partition plate I, wherein the oxidation flocculation area is communicated with the spraying area, the top of the circulating clear liquid area completely separates the circulating clear liquid area from the oxidation flocculation area and the spraying area through a partition plate II, and a vent is arranged on the tower wall at the top of the circulating clear liquid area; the partition plate I is provided with at least one opening, and the area of the opening is 10% -90% of that of the partition plate I; a filter medium is fixed on the opening of the clapboard I; the bottom of the oxidation flocculation area is connected with a flue gas pipeline II and an outer discharging slurry pipeline; the flue gas pipeline II extends to the inside of the oxidation flocculation area and is parallel to the partition plate I, and a plurality of groups of flue gas branch pipes are sequentially and horizontally distributed on the flue gas pipeline II from bottom to top in the oxidation flocculation area; each group of flue gas branch pipes consists of 2-8 flue gas branch pipes, each flue gas branch pipe is arc-shaped, and each group of flue gas branch pipes are uniformly distributed in the horizontal direction and have the same rotating direction; a plurality of large-caliber atomizing nozzles with upward or downward openings are axially arranged at the upper part of the rapid cooling and cooling zone, each large-caliber atomizing nozzle is connected with a clean water branch pipe, and the clean water branch pipe is connected with a clean water main pipe; the ratio of the pipe diameter of an inlet joint of the large-diameter atomizing nozzle to the tower diameter of the quenching and cooling area is 0.005-0.1; the spraying angle of the large-diameter atomizing nozzle is 60-150 degrees.
2. The flue gas desulfurization tower of claim 1, wherein: the filter medium is of a net structure, and the size of the meshes is 0.1-1000 mu m; the material of the filter medium is natural fiber, synthetic fiber, glass fiber or metal wire.
3. The flue gas desulfurization tower of claim 1, wherein: the two ends of the partition plate II are respectively connected with the partition plate I and the tower wall of the circulating clear liquid area, and the included angle of the joint of the partition plate I and the partition plate II is 45-165 degrees.
4. The flue gas desulfurization tower of claim 1, wherein: the flue gas emission area and the demisting area are connected through the conical reducing, and the tower diameter ratio of the demisting area to the flue gas emission area is 1.2-5.
5. The flue gas desulfurization tower of claim 1, wherein: the tower disc area is connected with the spraying area through the inverted cone-shaped reducing area; the tower diameter ratio of the tower tray area to the spraying area is 1.2-3.
6. The flue gas desulfurization tower of claim 1, wherein: the demisting device is one or more of a cyclone demister, a wet electrostatic demister, a wire mesh demister or a baffling demister.
7. The flue gas desulfurization tower of claim 1, wherein: and a liquid distributor is arranged between the tower tray area and the demisting area, and is connected with a circulating clear liquid pipeline I and used for uniformly distributing circulating clear liquid on the tower tray.
8. The flue gas desulfurization tower of claim 1, wherein: one or more layers of spraying pipelines are arranged at the upper part of the spraying area; when a plurality of layers of spraying pipelines are arranged, the distance between the spraying pipelines is 0.5-5 m; the spraying pipeline is connected with a circulating clear liquid pipeline II, and a plurality of atomizing nozzles are arranged on the spraying pipeline.
9. The flue gas desulfurization tower of claim 1, wherein: the rapid cooling and cooling zone at least comprises a pair of large-caliber atomizing nozzles with opposite openings.
10. The flue gas desulfurization tower of claim 1, wherein: one side of the oxidation flocculation area, which is close to the tower wall, is respectively connected with an alkaline solution pipeline I, a flocculating agent pipeline and a liquid level meter I; and the alkaline solution pipeline I is provided with a flow regulating valve.
11. The flue gas desulfurization tower of claim 1, wherein: one side of the circulating clear liquid zone, which is close to the tower wall, is connected with a fresh water pipeline, an alkaline solution pipeline II, an oxidizing gas pipeline and a liquid level meter II; a flow regulating valve is arranged on the fresh water pipeline; and the alkaline solution pipeline II is provided with a flow regulating valve for regulating the flow of the alkaline solution filled into the circulating clear liquid area.
12. The flue gas desulfurization tower of claim 11, wherein: the oxidizing gas pipeline is connected with the fan, extends to one side of the partition plate I of the circulating clear liquid zone and is connected with the oxidizing gas distribution pipe; the oxidizing gas distribution pipe is provided with a plurality of nozzles, and the nozzles are opposite to the filter medium on the partition plate I.
13. The flue gas desulfurization tower of claim 1, wherein: the bottom of the circulating clear liquid zone is connected with a clear liquid leading-out pipeline, the leading-out pipeline is divided into two paths, one path of pipeline is connected with an external clear liquid discharging pipeline, the other path of pipeline is connected with a circulating clear liquid pump, a pH meter is arranged on the pipeline, and the circulating clear liquid pump is connected with a circulating clear liquid pipeline I and a circulating clear liquid pipeline II through a cooler; the pH meter is used for measuring the pH value of the circulating clear liquid and feeding back a measurement signal to the regulating valve of the alkaline solution pipeline II through the controller.
14. A flue gas dedusting, desulfurizing and wastewater treatment process of the flue gas desulfurization tower of any one of claims 1 to 13, characterized by comprising the following steps: (1) flue gas enters a flue gas desulfurization tower in two paths, one path of flue gas enters from the lower part of a quenching and cooling area of the flue gas desulfurization tower through a flue gas pipeline I, the other path of flue gas enters from the bottom of an oxidation and flocculation area of the flue gas desulfurization tower through a flue gas pipeline II after being pressurized and passes through slurry in the oxidation and flocculation area, the two paths of flue gas are converged and then contact with clean water atomized by the quenching and cooling area to carry out quenching and cooling, the quenched and cooled flue gas enters a spraying area and is in countercurrent contact with circulating clear liquid in the spraying area to remove most of dust and sulfur dioxide carried in the flue gas, the flue gas passing through the spraying area enters a tower panel area, deep dedusting and desulfurization are carried out on the tower panel area and the circulating clear liquid, and the purified flue gas is demisted by a demisting area and then is discharged from a flue gas discharge area; (2) the desulfurization slurry absorbing the dust and the sulfur dioxide enters an oxidation flocculation area, and is fully mixed with oxidizing gas, a flocculating agent and an alkaline solution under the stirring action of the flue gas entering through a flue gas pipeline II, sulfite in the desulfurization slurry is oxidized into sulfate, small particle dust in the desulfurization slurry is flocculated into large particles, and meanwhile, the flue gas with a certain temperature enables the moisture in the desulfurization slurry to be continuously volatilized, and the salt concentration is gradually increased; (3) the desulfurization slurry flows through a filter medium on a partition plate I to realize solid-liquid separation under the action of liquid level difference on two sides of the partition plate I, dust particles in the desulfurization slurry are filtered and left in an oxidation flocculation area, clear liquid enters a circulating clear liquid area, and the slurry after oxidation flocculation is led out from the bottom of the oxidation flocculation area and enters a subsequent treatment unit through an external slurry pipeline; (4) oxidizing gas enters from the circulating clear liquid zone, is sprayed out from a nozzle of the oxidizing gas distribution pipe and penetrates through the filter medium, dust particles on the filter medium of the oxidation flocculation zone are blown up, the blown-up dust and the oxidizing gas are taken away by the rotating slurry, the dust and a flocculating agent are aggregated into large particles under the action of gravity and are deposited at the bottom of the oxidation flocculation zone, sulfite in the slurry is oxidized into sulfate by the oxidizing gas, and COD of the desulfurization wastewater reaches the standard; (5) the clear liquid which is filtered by the filter medium and enters the circulating clear liquid area is mixed with fresh water and alkaline solution in the circulating clear liquid area and then is led out from the bottom of the circulating clear liquid area, a small amount of clear liquid is directly discharged to reduce the salt concentration of the circulating clear liquid, the rest clear liquid enters the cooler after being pressurized by the circulating clear liquid pump, one part of the clear liquid cooled by the cooler enters the spraying area, is atomized by the atomizing nozzle and then is in countercurrent contact with the flue gas to remove dust and sulfur, the other part of the clear liquid flows through the liquid distributor and enters the tower disc area to be in full contact with the flue gas on the tower disc, and a large amount of micro fog drops carried by the spraying area are captured by the micro dust particles and the flue gas.
15. The process according to claim 14, characterized in that: the flue gas in the step (1) is one or more of flue gas of a coal-fired boiler, flue gas of a coal-fired power plant, regenerated flue gas of a catalytic cracking catalyst, flue gas of a process heating furnace, coking flue gas or steel sintering flue gas.
16. The process according to claim 14, characterized in that: the ratio of the amount of the flue gas entering the flue gas pipeline I to the amount of the flue gas entering the flue gas pipeline II is 20-500; the ratio of clean water to flue gas in the quenching and cooling zone is 0.05-2.5L/Nm3(ii) a The ratio of the circulating clear liquid to the flue gas in the spraying area is 5-50L/Nm3And the ratio of the circulating clear liquid to the flue gas in the tower tray area is 3-15L/Nm3。
17. The process according to claim 14, characterized in that: the content of soluble salt in the clean water is less than or equal to 30 g/L.
18. The process according to claim 14, characterized in that: the alkaline solution is selected from one or more of sodium hydroxide solution, calcium hydroxide solution, magnesium hydroxide solution, sodium carbonate solution, sodium sulfite solution, sodium citrate solution, limestone slurry, ammonia water or seawater.
19. The process according to claim 14, characterized in that: the oxidizing gas is one or more of air, oxygen or ozone.
20. The process according to claim 14, characterized in that: the flocculating agent is one or more of aluminum sulfate, alum, sodium aluminate, ferric trichloride, ferrous sulfate, ferric sulfate, polyaluminum chloride, polyaluminum sulfate, polyaluminum phosphate, polyaluminum chloride, polyferric sulfate, polyaluminum phosphate, polyphosphazene chloride, polyaluminum phosphate chloride, polysilicate iron, polysilicate ferric sulfate, polyaluminum sulfate silicate, polyaluminum ferric sulfate chloride, polyaluminum ferric silicate flocculating agent, aluminum-iron copolymerization composite flocculating agent, polysilicate flocculating agent or polyacrylamide flocculating agent.
21. The process according to claim 14, characterized in that: and (4) controlling the pH value of the slurry after the oxidative flocculation concentration in the step (3) to be 7-9, wherein an online pH detector is positioned on an external slurry discharge pipeline, and the pH value of the desulfurized slurry is controlled by adjusting an adjusting valve on an alkaline solution pipeline I.
22. The process according to claim 14, characterized in that: and (4) the liquid level difference between the two sides of the partition plate I in the step (3) is 0.5-6 m, and the liquid level of the oxidation flocculation area is higher than that of the circulating clear liquid area.
23. The process according to claim 14, characterized in that: and (4) controlling the liquid level height of the oxidation flocculation area in the step (3) by an adjusting valve on an external slurry discharge pipeline.
24. The process according to claim 14, characterized in that: and (4) periodically washing the filter medium on the partition plate I by using a washing water spraying pipe in the oxidation flocculation area in the step (3), wherein the washing time interval is 0.5-2 h.
25. The process according to claim 14, characterized in that: and (4) controlling the liquid level height of the circulating clear liquid area in the step (3) by an adjusting valve on a fresh water pipeline.
26. The process according to claim 14, characterized in that: and (5) controlling the pH value of the circulating clear liquid area in the steps (3) to (5) to be 6-11, wherein an online pH detector is positioned on an inlet pipeline of a circulating pump at the bottom of the tower, and the pH value of the circulating clear liquid is controlled by adjusting an adjusting valve on an alkaline solution pipeline II.
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