CN203370453U - Fume treatment equipment - Google Patents
Fume treatment equipment Download PDFInfo
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- CN203370453U CN203370453U CN201320342751.2U CN201320342751U CN203370453U CN 203370453 U CN203370453 U CN 203370453U CN 201320342751 U CN201320342751 U CN 201320342751U CN 203370453 U CN203370453 U CN 203370453U
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- sulfur dioxide
- flue gas
- zinc oxide
- dioxide absorption
- absorption
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- 239000003517 fume Substances 0.000 title abstract 8
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 263
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims abstract description 146
- 238000010521 absorption reaction Methods 0.000 claims abstract description 103
- 239000011787 zinc oxide Substances 0.000 claims abstract description 45
- 238000004537 pulping Methods 0.000 claims abstract description 18
- 239000002245 particle Substances 0.000 claims abstract description 12
- 235000010269 sulphur dioxide Nutrition 0.000 claims description 126
- 239000003546 flue gas Substances 0.000 claims description 117
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 116
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 22
- 229910052760 oxygen Inorganic materials 0.000 claims description 22
- 239000001301 oxygen Substances 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 19
- 239000007921 spray Substances 0.000 claims description 13
- 238000005507 spraying Methods 0.000 claims description 12
- 239000000706 filtrate Substances 0.000 claims description 9
- 238000003825 pressing Methods 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 6
- 239000004291 sulphur dioxide Substances 0.000 claims description 5
- 239000012065 filter cake Substances 0.000 claims description 3
- 238000010276 construction Methods 0.000 claims 1
- 238000011085 pressure filtration Methods 0.000 claims 1
- 230000003009 desulfurizing effect Effects 0.000 abstract 1
- 238000006477 desulfuration reaction Methods 0.000 description 29
- 230000023556 desulfurization Effects 0.000 description 29
- 239000002002 slurry Substances 0.000 description 27
- 238000006243 chemical reaction Methods 0.000 description 19
- 239000007788 liquid Substances 0.000 description 19
- 239000006227 byproduct Substances 0.000 description 12
- 239000007787 solid Substances 0.000 description 9
- 239000007789 gas Substances 0.000 description 7
- 238000007254 oxidation reaction Methods 0.000 description 7
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 description 7
- 229960001763 zinc sulfate Drugs 0.000 description 7
- 229910000368 zinc sulfate Inorganic materials 0.000 description 7
- HSYFJDYGOJKZCL-UHFFFAOYSA-L zinc;sulfite Chemical compound [Zn+2].[O-]S([O-])=O HSYFJDYGOJKZCL-UHFFFAOYSA-L 0.000 description 7
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 6
- 230000003647 oxidation Effects 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 230000002745 absorbent Effects 0.000 description 5
- 239000002250 absorbent Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 230000002035 prolonged effect Effects 0.000 description 5
- 239000008187 granular material Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- 238000005868 electrolysis reaction Methods 0.000 description 3
- 239000011701 zinc Substances 0.000 description 3
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 229910052725 zinc Inorganic materials 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
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Abstract
The utility model provides fume treatment equipment. The fume treatment equipment comprises a pulping device and a sulfur dioxide absorption device, wherein the pulping device is suitable for pulping zinc oxide particles so as to obtain zinc oxide slurry; the sulfur dioxide absorption device is connected with the pulping device, and treats fume containing sulfur dioxide by using the zinc oxide slurry, so as to absorb sulfur dioxide in the fume; the sulfur dioxide absorption device comprises an absorption device body, a sprayer and a fume inlet, wherein the sprayer and the fume inlet are configured to be the mode that at least part of the zinc oxide slurry is in countercurrent contact with part of the fume. Thus, by using the equipment, equipment clogging can be effectively avoided, and at the same time, high desulfurizing efficiency can be achieved.
Description
Technical Field
The utility model relates to a chemical industry field, it is specific, the utility model relates to a flue gas treatment device.
Background
The existing zinc oxide method for removing sulfur dioxide in flue gas is not a lot of examples, the existing absorption towers are turbulent ball towers, efficient scrubbers, DS-multiphase reactors and the like, some absorption towers are closed or modified, some absorption towers are still in operation, the devices in operation also frequently break down, the normal operation is difficult to maintain, and the treatment efficiency is obviously reduced.
Therefore, the method for removing sulfur dioxide in flue gas by zinc oxide method and the equipment thereof are still to be further improved.
SUMMERY OF THE UTILITY MODEL
The utility model discloses aim at solving one of the technical problem that exists among the prior art at least. Therefore, an object of the utility model is to provide a flue gas treatment device, this equipment have empty tower and spray the flue gas treatment device of structure, and this equipment can absorb the sulfur dioxide gas in the flue gas effectively, can effectively overcome the shortcoming that other equipment easily blockked up, can reach higher desulfurization efficiency simultaneously.
In one aspect of the present invention, the utility model provides a flue gas treatment device. According to the utility model discloses an embodiment, this flue gas treatment equipment includes: the pulping device is suitable for carrying out size mixing treatment on the zinc oxide particles so as to obtain zinc oxide slurry; the sulfur dioxide absorbing device is connected with the pulping device and used for treating the flue gas containing sulfur dioxide by using the zinc oxide slurry so as to absorb the sulfur dioxide in the flue gas, wherein the sulfur dioxide absorbing device comprises: the absorption device comprises an absorption device body, wherein a sulfur dioxide absorption space is defined in the absorption device body; the sprayer is arranged in the sulfur dioxide absorption space, is connected with the pulping device and is used for spraying the zinc oxide slurry into the sulfur dioxide absorption space; and the flue gas inlet is arranged on the absorption device body and is used for introducing flue gas containing sulfur dioxide into the sulfur dioxide absorption space, wherein the sprayer and the flue gas inlet are arranged, and at least one part of the zinc oxide slurry is in countercurrent contact with at least one part of the flue gas.
Utilize above-mentioned flue gas treatment facility can effectively reach the purpose that carries out the desorption to sulfur dioxide in the flue gas, especially utilize this equipment to have the sulfur dioxide absorption space of proper amount size, adopt empty tower to spray the design, on the one hand the at utmost reduces to block up, and on the other hand spray column resistance is low, and gaseous resistance loss also very reduces, can reach higher desulfurization efficiency simultaneously. The sprayer in the equipment enables the zinc oxide slurry to contact with the flue gas in a spraying mode, and the zinc oxide slurry sprayed out from the sprayer can be in countercurrent contact with the flue gas to the maximum extent through the position of the sprayer and the position of the flue gas inlet, so that the reaction time of sulfur dioxide and zinc oxide in the flue gas can be prolonged, and the desulfurization efficiency can be further improved.
In addition, according to the utility model discloses an above-mentioned flue gas treatment device can also have following additional technical characterstic:
the utility model discloses in, follow sulfur dioxide absorbing device's axial direction, the sprayer sets up the top of flue gas entry. Thereby prolonging the contact time of the zinc oxide slurry and the flue gas to the maximum extent.
The utility model discloses in, the sprayer is multilayer spray plate structure. Thereby, the zinc oxide slurry can be fully contacted with the flue gas.
In the present invention, the sulfur dioxide absorption device further comprises: and the demister is arranged in the sulfur dioxide absorption space. Thereby reducing entrainment of droplets of the slurry.
The utility model discloses in, follow sulfur dioxide absorbing device's axial direction, the defroster sets up the below of flue gas entry. Therefore, the de-misting can be carried out on the zinc oxide slurry after absorbing the sulfur dioxide, so as to reduce the entrainment of the droplets of the slurry.
In the present invention, the demister is a baffle plate. Whereby the defogging efficiency can be further improved.
The utility model discloses in, including a plurality of sulfur dioxide absorption device of establishing ties. Thereby, low pH gradient control can be realized.
The utility model discloses in, above-mentioned flue gas treatment facility can also include: and the filter pressing device is connected with the sulfur dioxide absorption device and is used for carrying out filter pressing treatment on the zinc oxide slurry which is in countercurrent contact with the flue gas so as to obtain a filter cake and filtrate. Thereby further completing the subsequent work of flue gas treatment.
The utility model discloses in, filter pressing device still links to each other with slurrying device, so that will filtrating is used for the size mixing is handled. Therefore, the full utilization of the filtrate can be improved, and the resource waste is avoided.
In the present invention, the sulfur dioxide absorption device may further include: and the oxygen inlet is arranged on the absorption device body and is used for supplying oxygen into the sulfur dioxide absorption space. According to an embodiment of the invention, the oxygen is provided in the form of air. Thereby providing oxygen to the desulfurization environment for the purpose of producing different byproducts.
The utility model discloses in, the granularity of zinc oxide granule is 150 ~ 400 meshes, can reach higher desulfurization efficiency from this.
The utility model discloses in, the solid content of zinc oxide thick liquid is 5 ~ 30 weight percent, can reach higher desulfurization efficiency from this.
In order to facilitate understanding of the above system, a method for removing sulfur dioxide from flue gas by using the above apparatus is described below, the method comprising: carrying out size mixing treatment on the zinc oxide particles so as to obtain zinc oxide slurry; and treating the flue gas containing sulfur dioxide by using the zinc oxide slurry so as to absorb the sulfur dioxide in the flue gas, wherein the zinc oxide slurry is in countercurrent contact with the flue gas containing sulfur dioxide in a spraying mode. The method can effectively remove sulfur dioxide in the flue gas, reduce blockage to the maximum extent and achieve higher desulfurization efficiency.
In the present invention, the above method further comprises: and carrying out desulfurization treatment on the flue gas containing the sulfur dioxide for multiple times so as to prepare multiple byproducts.
In the utility model, the concentration of sulfur dioxide in the flue gas is more than 1000mg/Nm 3. According to an embodiment of the present invention, the zinc oxide slurry has a zinc oxide content of 5 to 30 wt%. According to an embodiment of the present invention, the average particle size of the solid particles in the zinc oxide slurry is 150 to 400 mesh. Whereby higher desulfurization efficiency can be further achieved.
In the utility model, the zinc oxide slurry and the flue gas containing sulfur dioxide are absorbed and treated in a liquid-gas ratio of 6-40L/m 3. Whereby higher desulfurization efficiency can be further achieved.
In the utility model, the zinc oxide slurry is in multi-layer spraying mode and the flue gas containing sulfur dioxide is in countercurrent contact. Therefore, the contact time of the zinc oxide slurry and the flue gas can be prolonged to the maximum extent, and the zinc oxide slurry and the flue gas can react fully, so that the desulfurization efficiency is further improved.
In the present invention, further comprising: contacting the zinc oxide slurry with the flue gas in the presence of oxygen. According to an embodiment of the invention, the oxygen is provided in the form of air. Thereby providing oxygen to the desulfurization environment for the purpose of producing different byproducts.
In the present invention, further comprising: and demisting the fog drops in the environment where the zinc oxide slurry is contacted with the flue gas containing sulfur dioxide.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The above and/or additional aspects and advantages of the present invention will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
fig. 1 is a schematic structural diagram of a flue gas treatment system according to an embodiment of the present invention.
Fig. 2 is a schematic structural diagram of a flue gas treatment system according to an embodiment of the present invention.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary only for the purpose of explaining the present invention, and should not be construed as limiting the present invention.
For convenience of understanding, the flue gas treatment system equipment according to the embodiment of the present invention, which can be used for implementing the above method for treating flue gas, is described in detail below with reference to fig. 1 to 2.
The utility model provides a flue gas processing system. According to the utility model discloses an embodiment, this flue gas processing system includes: the device comprises a pulping device 100 and a sulfur dioxide absorption device 200, wherein the sulfur dioxide absorption device 200 is connected with the pulping device 100.
According to the utility model discloses a concrete embodiment, slurrying device 100 is suitable for and carries out the size mixing processing to the zinc oxide granule to obtain the zinc oxide thick liquid, the zinc oxide thick liquid is arranged in adsorbing the sulfur dioxide in the flue gas. According to the specific embodiment of the present invention, the sulfur dioxide absorption device 200 utilizes the zinc oxide slurry prepared by the above-mentioned pulping device 100 to treat the flue gas containing sulfur dioxide so as to absorb the sulfur dioxide in the flue gas.
The principle of absorbing sulfur dioxide by using the zinc oxide slurry is as follows: the material containing zinc oxide is used for preparing zinc oxide absorption slurry, the zinc oxide absorption slurry is contacted with the flue gas containing sulfur dioxide in a sulfur dioxide absorption device 200, and the zinc oxide is removed in the form of zinc sulfite and zinc sulfate by utilizing the reaction of the zinc oxide and the sulfur dioxide. The zinc sulfite recovers sulfur dioxide and zinc oxide through thermal decomposition or acid decomposition, and the zinc sulfate can be sent to a zinc electrolysis workshop for electrolysis or evaporative crystallization to obtain a solid. The reaction formula of the zinc oxide method desulfurization is as follows:
SO2dissolving in water: SO (SO)2+H2O＝HSO3 -+H+(1)
HSO3 -＝SO3 2-+H+(2)
ZnO reaction: ZnO +2H+→Zn2++H2O(3)
Zn2++SO3 2-+5/2H2O＝ZnSO3·5/2H2O(4)
ZnSO3·5/2H2O+H+＝Zn2++HSO3 -+5/2H2O(5)
According to the embodiment of the present invention, the above reactions all occur in the sulfur dioxide absorption device 200, and if the by-product zinc sulfite is required to be produced more, the reaction conditions are enhanced to make the reaction (4) become the main reaction and simultaneously suppress the reaction (5). No matter which process or equipment is adopted for realizing the reactions, proper conditions are created to ensure that the reactions are carried out in a favorable direction, the reaction speed is increased as much as possible, and the desulfurization efficiency is improved.
According to the utility model discloses a concrete embodiment, above-mentioned slurrying device 100 prepares into the zinc oxide thick liquids with the material that contains zinc oxide, wherein, according to the utility model discloses a concrete example, the zinc oxide content is 5 ~ 30 weight% in the zinc oxide thick liquids is obtained in the preparation. According to the utility model discloses a specific embodiment, the average particle size of zinc oxide granule is 150 ~ 400 meshes, can further reach higher desulfurization efficiency from this.
According to an embodiment of the present invention, the sulfur dioxide absorption device 200 may further include an absorption device body 210, and a sulfur dioxide absorption space is defined in the absorption device body 210. Thus, the flue gas containing sulfur dioxide is removed in a sulfur dioxide space by means of a zinc oxide slurry. Therefore, the sulfur dioxide absorption space is of an empty tower structure, so that the device can be prevented from being blocked, and higher desulfurization efficiency can be achieved.
According to an embodiment of the present invention, the sulfur dioxide absorption device 200 can further comprise a sprayer 220, the sprayer 220 is disposed in the sulfur dioxide absorption space and connected to the pulping device 100, for spraying the zinc oxide slurry to the sulfur dioxide absorption space.
According to an embodiment of the present invention, the sulfur dioxide absorption device 200 can further include a flue gas inlet 230, the flue gas inlet 230 is disposed on the absorption device body, and is used for introducing the flue gas containing sulfur dioxide into the sulfur dioxide absorption space. According to an embodiment of the present invention, the sprayer 220 and flue gas inlet 230 are configured such that at least a portion of the zinc oxide slurry is in counter-current contact with at least a portion of the flue gas. Therefore, the contact time of the zinc oxide slurry and the flue gas containing sulfur dioxide can be further prolonged, and the zinc oxide slurry has enough time to fully react, so that the sulfur dioxide in the flue gas can be removed to the maximum extent, and the removal efficiency of the sulfur dioxide is improved.
To this end, according to an embodiment of the present invention, as shown in fig. 1, the sprayer 220 may be disposed above the flue gas inlet 230 in the axial direction of the sulfur dioxide absorbing device 100. The flue gas enters the sulfur dioxide absorption device 100 from the flue gas inlet 230 and runs towards the flue gas outlet 231 arranged at the upper part of the device 100, and zinc oxide slurry sprayed downwards from a sprayer arranged above the flue gas inlet is encountered in the process, so that the flue gas and the zinc oxide slurry are in countercurrent contact, the contact time of the zinc oxide slurry and the flue gas containing sulfur dioxide can be further prolonged, the flue gas containing sulfur dioxide can be reacted sufficiently, the sulfur dioxide in the flue gas can be removed to the maximum extent, and the removal efficiency of the sulfur dioxide is improved.
According to the utility model discloses an embodiment, spray thrower 220 is multilayer spray plate structure, can spray sufficient zinc oxide thick liquid to sulfur dioxide in absorbing the space from this to the sulfur dioxide in the abundant desorption flue gas. According to the utility model discloses a specific embodiment, the sulfur dioxide thick liquid that the sprayer 220 that is multilayer spray plate structure sprayed can cover the horizontal area in whole sulfur dioxide absorption space, can make the flue gas can fully contact with zinc oxide thick liquid from this to further improve sulfur dioxide's desorption efficiency.
According to an embodiment of the present invention, the sulfur dioxide absorption device 100 may further include: a demister 240, the demister 240 being disposed within the sulfur dioxide absorbing space. Can utilize this defroster 240 to carry out the defogging to the zinc oxide thick liquid after absorbing the sulfur dioxide from this, according to the utility model discloses a specific embodiment, defroster 240 sets up the below at the flue gas entry to reduce the fog droplet of thick liquid and smuggle secretly. According to the utility model discloses a specific example, the concrete type ratio of defroster 240 is not restricted very much, as long as can have the defogging function can, according to the utility model discloses a specific example, defroster 240 can be for the baffling board, can further improve the defogging effect from this, reduces the droplet of thick liquid and smugglies secretly, reduces the thick liquid and follows the environment secondary pollution that the flue gas effusion caused.
According to an embodiment of the present invention, the flue gas treatment apparatus may comprise a plurality of sulphur dioxide absorption devices 200 in series. According to the utility model discloses a concrete embodiment can set up sulfur dioxide absorbing device 200 doublestage or tertiary series connection and use, realizes low pH value gradient control, and different sulfur dioxide absorbing device 200 focus on different functions, can reach the requirement that satisfies desulfurization efficiency and production qualified by-product simultaneously. The primary absorption device has the main functions of oxidizing part of oxygen, concentrating filtrate to reach the specified zinc sulfate concentration, promoting the dissolution of zinc oxide and removing part of sulfur dioxide, so that the pH value in the absorption device system is slightly lower, and the oxidation and dissolution processes are facilitated; the secondary absorption device has the main function of ensuring the absorption effect of sulfur dioxide and meeting the requirement of environmental protection, so that the pH value in the device is slightly higher, and the absorption process of sulfur dioxide from a gas phase to a liquid phase is facilitated.
According to the utility model discloses an embodiment, above-mentioned flue gas treatment facility can also include: and the filter pressing device 250 is connected with the sulfur dioxide absorption device 200 and is used for carrying out filter pressing treatment on the zinc oxide slurry which is in countercurrent contact with the flue gas so as to obtain a filter cake and filtrate. Thereby further completing the subsequent work of flue gas treatment.
According to an embodiment of the present invention, the filter press device 250 is further connected to the slurrying device 100 so as to use the filtrate for the slurry conditioning treatment. Therefore, the full utilization of the filtrate can be improved, and the resource waste is avoided.
According to the embodiment of the present invention, the sulfur dioxide absorption device 200 may further include an oxygen inlet 260, the oxygen inlet 260 is disposed on the absorption device body for supplying oxygen into the sulfur dioxide absorption space. According to an embodiment of the invention, the oxygen is provided in the form of air. Thereby providing oxygen to the desulfurization environment for the purpose of producing different byproducts. Specifically, after oxygen is introduced, the oxygen reacts with the sulfur dioxide aqueous solution to obtain zinc sulfate. The specific reaction is as follows:
and (3) oxidation reaction: 2HSO3 -+O2→2SO4 2-+2H+(6)
ZnSO3·5/2H2O+1/2O2→Zn2++SO4 2-+5/2H2O(7)
Therefore, according to the embodiment of the present invention, if the by-product zinc sulfate is produced more, the reaction conditions are strengthened to make the reaction (6) and the above-mentioned reaction (5) and the main reaction, and the above-mentioned reaction (4) is suppressed. No matter which process or equipment is adopted for realizing the reactions, proper conditions are created to ensure that the reactions are carried out in a favorable direction, the reaction speed is increased as much as possible, and the desulfurization efficiency is improved.
In order to facilitate understanding of the flue gas treatment system of the present invention, the following description specifically describes the specific operation steps for treating flue gas containing sulfur dioxide by using the flue gas treatment equipment.
According to the utility model discloses a concrete embodiment, the utility model discloses a flue gas processing system is suitable for the SO in the absorption flue gas2Can be used at 1000mg/Nm3The sulfur dioxide flue gas with the above concentration is especially 5000mg/Nm3The sulfur dioxide flue gas with the concentration higher than that is more suitable.
Analysis of the condition of the absorbent: screening a proper zinc oxide absorbent from available zinc oxide, and determining design operation parameters such as zinc oxide utilization rate, absorbent preparation concentration, slurry control concentration in a tower, pipeline specification and the like according to the components (the purity is usually 40-80%) and the granularity (usually 150-400 meshes) of the selected zinc oxide absorbent;
pulping: the zinc oxide absorbent and water are made into zinc oxide slurry with a certain concentration in the slurry making device 100, and the zinc oxide slurry is conveyed to the slurry storage tank through the slurry making tank pump for standby. Fresh zinc oxide slurry is sent into the sulfur dioxide absorption device 200 through a slurry delivery pump to remove sulfur dioxide gas in the flue gas, specifically, the sulfur dioxide absorption device 200 can adopt an absorption tower, and the amount of the supplemented fresh slurry can be adjusted according to the pH value in the absorption tower.
Absorption: according to the embodiment of the present invention, the sulfur dioxide absorption device 200 can be a plurality of series-connected devices 200, and the following sulfur dioxide absorption device 200 using two series-connected devices can be used to perform desulfurization treatment on flue gas by using two towers. According to the utility model discloses a concrete embodiment, the middle part that contains the sulfur dioxide flue gas and get into first absorption tower sprays the zinc oxide thick liquid countercurrent contact that gets off with the top of the tower, and flue gas temperature reduces after flue gas and thick liquid contact, and sulfur dioxide content wherein reduces, and the water content rises. And fog drops are removed by the first-stage baffle plate demister, then the fog drops enter the middle part of the second absorption tower, and then the fog drops are in countercurrent contact with zinc oxide slurry sprayed on the top of the tower, so that a chemical reaction is further carried out to absorb sulfur dioxide gas in the flue gas. The purified flue gas is subjected to fog drop removal by a two-stage demister at the top of the absorption tower, then leaves the absorption tower and is directly discharged by a chimney, and the emission concentration of sulfur dioxide reaches the national or local environmental protection standard. In order to maintain the zinc balance, the sulfur balance and the water balance in the absorption tower and ensure the normal operation of an absorption system, a certain amount of slurry is continuously led out from the absorption tower, the slurry mainly contains zinc sulfite solid, dissolved zinc sulfate, excessive zinc oxide, solid impurities, water and the like, and the discharged slurry is determined to be sent to a previous-stage absorption tower or a filtering device according to the pH value controlled by each tower.
According to the utility model discloses a concrete embodiment, the basic structure and the basic action of each absorption tower of absorption process are unanimous, the main characterized in that:
a. the liquid holdup of the tower kettle, namely the mixed solution stored at the bottom of the absorption tower after the zinc oxide slurry reacts with the flue gas, is stirred by a side-entry stirrer so as to prevent the slurry from settling, and the height of the liquid holdup of the tower kettle is related to the removal amount of sulfur dioxide and the oxidation requirement of zinc sulfite;
b. the circulating system adopts a unit system design, each spraying layer comprises a circulating pump, a pipeline system, a spraying assembly and a nozzle, and the circulating pump 270 connected with the spraying pipeline is matched, so that the coverage rate of more than 200% of absorption slurry in the absorption tower is ensured, and the nozzles of the sprayer 220 adopt a specific form to reduce the occurrence of blockage to the greatest extent;
c. the demister 240 adopts a baffle plate type to remove the entrained fog drops in the air flow and then discharge the air flow out of the absorption tower, and except that the last absorption tower is provided with two layers of demisters, other absorption towers only need one layer of demister;
d. oxidation of zinc sulfite: the air jet pipe is arranged at the front side of the side-entering stirrer, and the injected air is crushed into fine bubbles by the slurry pushed by the stirrer and well dispersed in the slurry;
e. the liquid-gas ratio of each absorption tower is 8-25L/m3Setting 2-5 slurry spraying layers according to the spraying requirement;
f. the pH value in the tower kettle is controlled to be 2-6, the solid content is controlled to be 5% -20%, and the oxidation rate of zinc sulfite is 10-80%.
The main difference in the function of the absorption towers connected in series is that:
a. controlling the pH value of the tower kettle in a gradient manner, wherein the pH value of the slurry is gradually increased according to the sequence of the passing of the flue gas;
b. the blowing of oxidizing air from one or both of the columns is determined according to the requirement of the by-product, and the control value of the solid content in the column needs to be set differently depending on whether the oxidation is required or not.
Filtering and separating slurry: the slurry discharged from the absorption tower can be subjected to solid-liquid separation by a filter press, and Zn in the filtrate2+The concentration of the waste water can be discharged when reaching a certain requirement (usually, the electrolysis concentration requirement is more than 100 g/L), and the waste water can not meet the concentration requirement and is returned to pulping. And carrying away the solid slag after filter pressing.
For the sake of understanding, the method for removing sulfur dioxide from flue gas by using the above-mentioned apparatus will be described in detail below, and the flue gas to be treated contains sulfur dioxide.
According to an embodiment of the present invention, the method may include: carrying out size mixing treatment on the zinc oxide particles so as to obtain zinc oxide slurry; and treating the flue gas containing sulfur dioxide by using the zinc oxide slurry so as to absorb the sulfur dioxide in the flue gas, wherein the zinc oxide slurry is in countercurrent contact with the flue gas containing sulfur dioxide in a spraying mode. Thereby, the desulfurization effect can be further improved.
According to an embodiment of the present invention, the method further comprises: the flue gas that contains sulfur dioxide carries out desulfurization treatment many times to prepare multiple by-product, can carry out desulfurization treatment many times simultaneously, can further improve desulfurization effect.
According to one embodiment of the invention, the concentration of sulphur dioxide in the flue gas is more than 1000mg/Nm 3. According to an embodiment of the present invention, the zinc oxide slurry has a zinc oxide content of 5 to 30 wt%. According to an embodiment of the present invention, the average particle size of the solid particles in the zinc oxide slurry is 150 to 400 mesh. From this can improve desulfurization effect through effective desulfurizer in the control thick liquid promptly zinc oxide's content and granularity, according to the utility model discloses a specific embodiment, the granule granularity can improve zinc oxide and sulfur dioxide's area of contact the less, can further improve desulfurization efficiency from this.
According to the utility model discloses an embodiment, will zinc oxide thick liquid and the flue gas that contains the sulfur dioxide carry out absorption treatment with the liquid-gas ratio of 6 ~ 40L/m 3. Thereby ensuring the absorption slurry coverage rate of more than 200 percent in the absorption tower, and the spray nozzle of the sprayer adopts a specific form to reduce the occurrence of blockage to the maximum extent, thereby further improving the desulfurization efficiency.
According to one embodiment of the present invention, the zinc oxide slurry is contacted with the flue gas containing sulfur dioxide in a multi-layer spray manner in a counter-current manner. Therefore, the contact time of the zinc oxide slurry and the flue gas can be prolonged to the maximum extent, the zinc oxide slurry and the flue gas are enabled to react fully, and higher desulfurization efficiency can be achieved.
According to the utility model discloses an embodiment, further include: contacting the zinc oxide slurry with the flue gas in the presence of oxygen. According to an embodiment of the invention, the oxygen is provided in the form of air. Thereby providing oxygen to the desulfurization environment for the purpose of producing different byproducts. According to the specific embodiment of the utility model, the oxidation air is supplied according to the requirement of the by-product, the air spray pipe is arranged at the front side of the side-entering type stirrer, and the sprayed air is crushed into fine bubbles by the slurry pushed by the stirrer and well dispersed in the slurry; the oxygen reacts with sulfur dioxide dissolved in water to generate zinc sulfate, so that the content of the oxygen can be controlled as required, and different byproducts can be prepared.
According to the utility model discloses an embodiment, further include: and demisting the fog drops in the environment where the zinc oxide slurry is contacted with the flue gas containing sulfur dioxide so as to reduce the entrainment of the fog drops of the slurry and reduce the secondary environmental pollution caused by the escape of the slurry along with the flue gas.
In the description herein, references to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., mean that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
While embodiments of the present invention have been shown and described, it will be understood by those of ordinary skill in the art that: various changes, modifications, substitutions and alterations can be made to the embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.
Claims (12)
1. A flue gas treatment apparatus, comprising:
the pulping device is suitable for carrying out size mixing treatment on the zinc oxide particles so as to obtain zinc oxide slurry;
the sulfur dioxide absorption device is connected with the pulping device and is used for treating the flue gas containing sulfur dioxide by using the zinc oxide slurry so as to absorb the sulfur dioxide in the flue gas,
wherein,
the sulfur dioxide absorption device comprises:
the absorption device comprises an absorption device body, wherein a sulfur dioxide absorption space is defined in the absorption device body;
the sprayer is arranged in the sulfur dioxide absorption space, is connected with the pulping device and is suitable for spraying the zinc oxide slurry into the sulfur dioxide absorption space;
a flue gas inlet arranged on the absorption device body and suitable for introducing flue gas containing sulfur dioxide into the sulfur dioxide absorption space,
wherein the sparger and flue gas inlet are arranged such that at least a portion of the zinc oxide slurry is in counter-current contact with at least a portion of the flue gas.
2. The plant according to claim 1, characterized in that the shower is arranged above the flue gas inlet in the axial direction of the sulphur dioxide absorption device.
3. The apparatus of claim 1, wherein the sprayer is of a multi-layer spray plate construction.
4. The plant of claim 1 wherein the sulfur dioxide absorption unit further comprises:
and the demister is arranged in the sulfur dioxide absorption space.
5. The plant according to claim 4, characterized in that the demister is arranged below the flue gas inlet in the axial direction of the sulphur dioxide absorption device.
6. The apparatus of claim 5, wherein the demister is a baffle.
7. The plant according to claim 1, comprising a plurality of sulphur dioxide absorption units in series.
8. The apparatus of claim 1, further comprising:
and the filter pressing device is connected with the sulfur dioxide absorption device and is suitable for carrying out filter pressing treatment on the zinc oxide slurry which is in countercurrent contact with the flue gas so as to obtain a filter cake and filtrate.
9. The apparatus according to claim 8, wherein said pressure filtration device is further connected to a pulping device for adapting said filtrate to said pulping process.
10. The plant of claim 1 wherein the sulfur dioxide absorption unit further comprises:
an oxygen inlet disposed on the absorption device body and adapted to supply oxygen into the sulfur dioxide absorption space.
11. The apparatus of claim 1, wherein the zinc oxide particles have an average particle size of 150 to 400 mesh.
12. The apparatus of claim 1, wherein the zinc oxide slurry has a zinc oxide content of 5 to 30 wt.%.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201320342751.2U CN203370453U (en) | 2013-06-14 | 2013-06-14 | Fume treatment equipment |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201320342751.2U CN203370453U (en) | 2013-06-14 | 2013-06-14 | Fume treatment equipment |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103349901A (en) * | 2013-06-14 | 2013-10-16 | 中国恩菲工程技术有限公司 | Flue gas processing method and device thereof |
| CN107261799A (en) * | 2017-07-20 | 2017-10-20 | 湖南辰州矿业有限责任公司 | A kind of device and method for preventing from smelting desulphurization system milk of lime fouling |
-
2013
- 2013-06-14 CN CN201320342751.2U patent/CN203370453U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103349901A (en) * | 2013-06-14 | 2013-10-16 | 中国恩菲工程技术有限公司 | Flue gas processing method and device thereof |
| CN103349901B (en) * | 2013-06-14 | 2016-07-06 | 中国恩菲工程技术有限公司 | Flue gas processing method and equipment thereof |
| CN107261799A (en) * | 2017-07-20 | 2017-10-20 | 湖南辰州矿业有限责任公司 | A kind of device and method for preventing from smelting desulphurization system milk of lime fouling |
| CN107261799B (en) * | 2017-07-20 | 2020-11-13 | 湖南辰州矿业有限责任公司 | Device and method for preventing lime milk of smelting desulfurization system from scaling |
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