CN212819076U - System for flue gas pollutant degree of depth desorption - Google Patents
System for flue gas pollutant degree of depth desorption Download PDFInfo
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- CN212819076U CN212819076U CN202020539839.3U CN202020539839U CN212819076U CN 212819076 U CN212819076 U CN 212819076U CN 202020539839 U CN202020539839 U CN 202020539839U CN 212819076 U CN212819076 U CN 212819076U
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Abstract
The utility model discloses a system for flue gas pollutant degree of depth desorption, from top to bottom has set gradually the defroster in the absorption tower, technology water spraying layer, the superfine spraying layer of filtrating water, alkali lye spraying layer, the thick liquid sprays the layer, tray and thick liquid pond, the top of absorption tower is provided with the exhanst gas outlet, the export of thick liquid pond is linked together through the entry on thick liquid circulating pump and thick liquid spraying layer, the export of technology water tank is linked together with the entry on technology water spraying layer, the export of filtrating water tank is linked together with the entry on the superfine spraying layer of filtrating water, the hourglass material mouth and the entry of calcium hydroxide solution preparation jar of lime storehouse bottom portion are linked together, the delivery port and the entry on alkali lye spraying layer of calcium hydroxide solution preparation jar, this system can promote the ability of wet flue gas desulfurization in coordination with the desorption dust by a wide margin, reduce the liquid-gas ratio in the absorption tower and the frequency that washes of defroster, area is little, and can avoid the export flue gas to carry the gypsum, the washing water yield is less simultaneously.
Description
Technical Field
The utility model belongs to the technical field of the environmental protection, a system of flue gas pollutant degree of depth desorption is related to.
Background
With the progress of environmental protection technology, the desulfurization technology is applied to more industrial waste gas generated by burning fossil energy to reduce the emission of sulfur dioxide in the waste gas. The wet desulfurization process is the most widely applied desulfurization technology at present, and the process utilizes a liquid desulfurizer to remove sulfur dioxide in flue gas.
The typical wet desulfurization process utilizes limestone as a desulfurizing agent, the main equipment of the process is an absorption tower, and flue gas enters the absorption tower from the middle part of the absorption tower and passes through a tray, a spraying layer, a demister and other removing equipment respectively. In the absorption tower, the flue gas is in countercurrent contact with a desulfurizing agent, and absorption reaction is carried out in the tower to generate CaSO3The calcium sulfite in the absorption tower is subjected to forced oxidation reaction to generate CaSO4Finally crystallizing the supersaturated gypsum solution to obtain the desulfurization byproduct gypsum (CaSO)4·2H2O) washing by an absorption towerThe purified flue gas passes through a demister at the top of the absorption tower to remove fine liquid drops brought by the desulfurized flue gas, and then is discharged into the atmosphere through a purified flue.
Due to the characteristics of the wet desulphurization process, the wet desulphurization process can not only effectively remove sulfur dioxide, but also has certain removal capacity on dust in flue gas. At present, only the removal of sulfur dioxide by the process is generally considered in the actual operation process of a wet desulphurization system, and the synergistic removal capability of the equipment to dust is not deeply considered. Due to the fact that the difference between the modification and the operation condition is large, the following problems generally exist in the existing wet desulphurization system: firstly, the system is complicated, the equipment volume is large, and the occupied area of the system is large; secondly, the liquid-gas ratio is too large, so that the energy consumption is high; the capability of the system for the cooperative dust treatment is not fully developed and utilized; fourthly, gypsum is carried by the flue gas at the outlet, so that the gypsum rain phenomenon appears at the discharge port of the chimney; the excessive washing water of demister and other equipment results in great process water consumption of the desulfurizing system.
The wet desulphurization is used as a mature desulphurization technology and widely applied to industrial production, and if the wet desulphurization process can be further optimized and modified, the synergistic dust removal capability of the wet desulphurization process is improved while the desulfurization efficiency is higher, the running power consumption and the material consumption are further reduced, the environmental protection is greatly contributed, and considerable economic benefits are brought to production enterprises.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome above-mentioned prior art's shortcoming, provide a system of flue gas pollutant degree of depth desorption, this system can promote the ability of wet flue gas desulfurization desorption dust in coordination by a wide margin, reduces the liquid-gas ratio in the absorption tower and the frequency of washing of defroster, and area is little, and can avoid exporting the flue gas to carry the gypsum, and the volume of washing water is less simultaneously.
In order to achieve the above purpose, the system for deeply removing the smoke pollutants comprises an absorption tower, wherein a demister, a process water spray layer, a filtrate water superfine spray layer, an alkali liquor spray layer, a slurry spray layer, a tray and a slurry pool are sequentially arranged in the absorption tower from top to bottom, the top of the absorption tower is provided with a smoke outlet, the outlet of the slurry pool is communicated with the inlet of the slurry spray layer through a slurry circulating pump, the outlet of a process water tank is communicated with the inlet of the process water spray layer, the outlet of a filtrate water tank is communicated with the inlet of the filtrate water superfine spray layer, a leakage port at the bottom of a quicklime bin is communicated with the inlet of a calcium hydroxide solution preparation tank, and the water outlet of the calcium hydroxide solution preparation tank is communicated with the inlet of the alkali liquor spray layer;
and a flue gas inlet is formed in the side surface of the absorption tower, wherein the flue gas inlet is positioned between the slurry pool and the tray.
The outlet of the process water tank is communicated with the inlet of the process water spray layer through a process water circulating pump.
The outlet of the filtrate water tank is communicated with the inlet of the filtrate water superfine spray layer through a filtrate water circulating pump.
The water outlet of the calcium hydroxide solution preparation tank is communicated with the inlet of the alkali liquor spraying layer through an alkali liquor circulating pump.
The flow rate of a single nozzle in the alkali liquor spraying layer is 3m3/h-5m3The spraying angle is 90-120 degrees, and the coverage rate is 100-150 percent.
The flow rate of a single nozzle in the superfine spray layer of the filtrate water is 0.05m3/h-0.15m3The spraying angle is 90-120 degrees, the coverage rate is 100-150 percent, and the spraying particle size is 150-300 mu m.
The flow rate of a single nozzle in the process water spray layer is 0.05m3/h-0.2m3The spraying angle is 90-120 degrees, the coverage rate is 100-150 percent, and the spraying particle size is 400-500 mu m.
The distance between the blades of the first layer of the blades in the demister is 10mm-20 mm.
The top of the calcium hydroxide solution preparation tank is provided with a heat exchange exhaust port.
The utility model discloses following beneficial effect has:
flue gas pollutant degree of depth desorption system when concrete operation, spray the flue gas after the layer washing through tray and thick liquid and carry out alkali lye spraying, the superfine spraying of filtrate water and technology water spraying to desorption dust in coordination, the spraying through superfine alkali lye, filtrate water and technology water simultaneously, with degree of depth desorption sulfur dioxide, and then reduce the circulation volume of normal thick liquid, reduce the use of circulating pump, reach the purpose that reduces the operation electric quantity. In addition, before the flue gas enters the demister, water spray is carried out to wash away gypsum slurry carried along with the flue gas, the slurry content in the flue gas is reduced, so that the washing frequency of the first-layer demister is reduced, and the consumption of process water is saved. And because the slurry content in the flue gas reduces, when carrying out first layer defroster design, can reduce its blade interval, increase substantially the ability that the defroster intercepted liquid drop and dust, reduce chimney outlet pollutant and discharge.
Drawings
Fig. 1 is a schematic structural view of the present invention;
fig. 2 is a schematic view of the spray layer arrangement of the present invention.
Wherein, 1 is an absorption tower, 2 is a flue gas inlet, 3 is a slurry circulating pump, 4 is a tray, 5 is a slurry spraying layer, 6 is a quicklime bin, 7 is a calcium hydroxide solution preparation tank, 8 is an alkali liquor circulating pump, 9 is a filtrate water tank, 10 is a filtrate water circulating pump, 11 is a process water tank, 12 is a process water circulating pump, 13 is an alkali liquor spraying layer, 14 is a filtrate water superfine spraying layer, 15 is a process water spraying layer, 16 is a demister, and 17 is a flue gas outlet.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings:
referring to fig. 1, the system for deeply removing smoke pollutants comprises an absorption tower 1, wherein a demister 16, a process water spray layer 15, a filtrate water ultrafine spray layer 14, an alkali liquor spray layer 13, a slurry spray layer 5, a tray 4 and a slurry pool are sequentially arranged in the absorption tower 1 from top to bottom, a flue gas outlet 17 is formed in the top of the absorption tower 1, an outlet of the slurry pool is communicated with an inlet of the slurry spray layer 5 through a slurry circulating pump 3, an outlet of a process water tank 11 is communicated with an inlet of the process water spray layer 15, an outlet of a filtrate water tank 9 is communicated with an inlet of the filtrate water ultrafine spray layer 14, a material leakage port at the bottom of a quicklime bin 6 is communicated with an inlet of a calcium hydroxide solution preparation tank 7, and a water outlet of the calcium hydroxide solution preparation tank 7 is communicated with an inlet of the alkali liquor spray layer 13; the side of the absorption tower 1 is provided with a flue gas inlet 2, wherein the flue gas inlet 2 is positioned between the slurry pool and the tray 4.
The outlet of the process water tank 11 is communicated with the inlet of the process water spray layer 15 through a process water circulating pump 12; the outlet of the filtrate water tank 9 is communicated with the inlet of the filtrate water superfine spray layer 14 through a filtrate water circulating pump 10; the water outlet of the calcium hydroxide solution preparation tank 7 is communicated with the inlet of the alkali liquor spraying layer 13 through an alkali liquor circulating pump 8.
The flow rate of a single nozzle in the alkaline solution spray layer 13 is 3m3/h-5m3The spraying angle is 90-120 degrees, and the coverage rate is 100-150 percent; the flow rate of a single nozzle in the filtrate water ultrafine spray layer 14 is 0.05m3/h-0.15m3The spraying angle is 90-120 degrees, the coverage rate is 100-150 percent, and the spraying particle size is 150-300 mu m; the flow rate of the individual nozzles in the process water spray 15 was 0.05m3/h-0.2m3The spraying angle is 90-120 degrees, the coverage rate is 100-150 percent, and the spraying particle size is 400-500 mu m; the distance between the blades of the first layer in each demister 16 is 10mm-20 mm; the top of the calcium hydroxide solution preparation tank 7 is provided with a heat exchange exhaust port.
The utility model discloses a concrete working process does:
the slurry in the slurry pool is pumped into a nozzle of the slurry spraying layer 5 by the slurry circulating pump 3, the slurry is atomized into liquid drops of about 2000 mu m by the nozzle and then falls down to be in countercurrent contact with the flue gas from bottom to top to absorb sulfur dioxide in the flue gas, and the chemical equation of the reaction generated in the absorption process is as follows:
SO3 2-+H+→HSO3 -
the slurry absorbing the flue gas finally falls into the slurry tank after passing through the tray 4, and the oxidation fan injects air into the slurry tank to perform oxidation reaction, so that gypsum crystals are finally separated out, wherein the chemical equation of the reaction is as follows:
SO3 2-+1/2O2→SO4 2-
HSO3 -+1/2O2→SO4 2-+H+
Ca2++SO3 2-+1/2H2O→CaSO3·1/2H2O(s)
Ca2++SO4 2-+2H2O→CaSO4·2H2O(s)
the quick lime raw materials are stored in a quick lime bin 6, the quick lime raw materials are conveyed to a calcium hydroxide solution preparation tank 7 below the quick lime bin 6 through a screw conveyor to prepare a calcium hydroxide solution, and heat generated when quick lime is dissolved is dissipated through a heat exchange exhaust port at the top of the calcium hydroxide solution preparation tank 7. The alkali liquor circulating pump 8 pumps the calcium hydroxide solution in the calcium hydroxide solution preparation tank 7 into a nozzle of the alkali liquor spray layer 13, the calcium hydroxide solution is atomized into 200-400 μm fog and then is in countercurrent contact with flue gas to absorb sulfur dioxide which is not captured by the slurry, the calcium hydroxide solution which absorbs the sulfur dioxide reacts to generate calcium sulfite, and finally the calcium sulfite and the slurry which absorbs the sulfur dioxide are oxidized in a slurry pool together, and finally gypsum crystals are separated out, wherein the main chemical equation of the reaction is as follows:
CaO+H2O→Ca(OH)2
SO2+Ca(OH)2→CaSO3+H2O
the filtrate water in the filtrate water tank 9 is pumped into a nozzle of the filtrate water superfine spray layer 14 by the filtrate water circulating pump 10, and the filtrate water is atomized into 200-300 mu m mist spray to be in countercurrent contact with the flue gas so as to absorb sulfur dioxide, dust and serous fluid in the flue gas.
At this time, the flue gas passes through the dust remover, the tray 4 and the spraying layer at the middle lower part of the absorption tower 1, so that most of dust and slurry fog drops carried in the flue gas are fine particles with very small particle size, and the trapping is mainly a brong diffusion mechanism at this time. The movement track of the dust and the fog drops is different from the streamline, the dust and the fog drops can shake around the streamline, and if the particulate matters are closer to the liquid drops, the particulate matters can collide with the liquid drops to be trapped. The smaller the particle size of the dust particles is, the stronger the Brown diffusion is, wherein the formula of the Brown diffusion and collection efficiency is as follows:
wherein eta isDFor trapping efficiency, Pe is the Peclet number and Re is the Reynolds number.
The process water circulating pump 12 pumps the process water in the process water tank 11 into the nozzles of the process water spray layer 15, the process water is atomized into 400-500 μm mist spray and then contacts with the flue gas in a countercurrent manner to absorb sulfur dioxide, dust and slurry in the flue gas, the trapping principle is the same as that of a filtrate water superfine spraying system, and the atomized droplets with larger particle size are conveniently trapped by the demister 16.
Slurry or other solid-liquid-containing droplets entering the demister 16 are obviously reduced through the paving of the alkali liquid spray layer 13, the filtrate water superfine spray layer 14 and the process water spray layer 15, so that the washing frequency of the demister 16 can be reduced, the distance between blades of the demister 16 at the first layer is reduced, and the capability of the demister 16 for intercepting droplets and dust is greatly improved.
Claims (9)
1. A system for deeply removing smoke pollutants is characterized by comprising an absorption tower (1), wherein, a demister (16), a process water spray layer (15), a filtrate water superfine spray layer (14), an alkali liquor spray layer (13), a slurry spray layer (5), a tray (4) and a slurry pool are sequentially arranged in the absorption tower (1) from top to bottom, the top of the absorption tower (1) is provided with a flue gas outlet (17), the outlet of the slurry pool is communicated with the inlet of the slurry spray layer (5) through a slurry circulating pump (3), the outlet of a process water tank (11) is communicated with the inlet of the process water spray layer (15), the outlet of a filtrate water tank (9) is communicated with the inlet of the filtrate water superfine spray layer (14), a material leakage port at the bottom of a quicklime bin (6) is communicated with the inlet of a calcium hydroxide solution preparation tank (7), and the water outlet of the calcium hydroxide solution preparation tank (7) is communicated with the inlet of the alkali liquor spray layer (13);
the side of the absorption tower (1) is provided with a flue gas inlet (2), wherein the flue gas inlet (2) is positioned between the slurry pool and the tray (4).
2. The system for the deep removal of pollutants from flue gas according to claim 1, wherein the outlet of the process water tank (11) is communicated with the inlet of the process water spray layer (15) through the process water circulating pump (12).
3. The system for the deep removal of pollutants in flue gas of claim 1, wherein the outlet of the filtrate water tank (9) is communicated with the inlet of the filtrate water ultrafine spray layer (14) through a filtrate water circulating pump (10).
4. The system for the deep removal of pollutants in flue gas according to claim 1, wherein a water outlet of the calcium hydroxide solution preparation tank (7) is communicated with an inlet of the alkali liquor spraying layer (13) through the alkali liquor circulating pump (8).
5. The system for deeply removing the pollutants in the flue gas according to claim 1, wherein the flow rate of a single nozzle in the alkaline solution spraying layer (13) is 3m3/h-5m3The spraying angle is 90-120 degrees, and the coverage rate is 100-150 percent.
6. The system for the deep removal of pollutants in flue gas according to claim 1, wherein the flow rate of a single nozzle in the ultrafine spray layer (14) of filtrate water is 0.05m3/h-0.15m3The spraying angle is 90-120 degrees, the coverage rate is 100-150 percent, and the spraying particle size is 150-300 mu m.
7. Root of herbaceous plantThe system for the deep removal of pollutants from flue gases according to claim 1, wherein the flow rate of a single nozzle in the process water spray layer (15) is 0.05m3/h-0.2m3The spraying angle is 90-120 degrees, the coverage rate is 100-150 percent, and the spraying particle size is 400-500 mu m.
8. The system for the deep removal of pollutants from flue gases according to claim 1, wherein the distance between the blades of the first layer in each blade of the demister (16) is 10mm-20 mm.
9. The system for the deep removal of pollutants from flue gas of claim 1, wherein the top of the calcium hydroxide solution preparation tank (7) is provided with a heat exchange exhaust port.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020539839.3U CN212819076U (en) | 2020-04-13 | 2020-04-13 | System for flue gas pollutant degree of depth desorption |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020539839.3U CN212819076U (en) | 2020-04-13 | 2020-04-13 | System for flue gas pollutant degree of depth desorption |
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| Publication Number | Publication Date |
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| CN212819076U true CN212819076U (en) | 2021-03-30 |
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| CN202020539839.3U Active CN212819076U (en) | 2020-04-13 | 2020-04-13 | System for flue gas pollutant degree of depth desorption |
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