CN113663489A - Treatment system and method for zinc leaching residue volatilizing kiln tail gas - Google Patents
Treatment system and method for zinc leaching residue volatilizing kiln tail gas Download PDFInfo
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- CN113663489A CN113663489A CN202110990025.0A CN202110990025A CN113663489A CN 113663489 A CN113663489 A CN 113663489A CN 202110990025 A CN202110990025 A CN 202110990025A CN 113663489 A CN113663489 A CN 113663489A
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- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 239000011701 zinc Substances 0.000 title claims abstract description 55
- 229910052725 zinc Inorganic materials 0.000 title claims abstract description 55
- 238000002386 leaching Methods 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000007789 gas Substances 0.000 claims abstract description 205
- 238000010521 absorption reaction Methods 0.000 claims abstract description 104
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 73
- 239000003513 alkali Substances 0.000 claims abstract description 57
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 40
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 claims abstract description 26
- 239000002245 particle Substances 0.000 claims abstract description 11
- 229910002651 NO3 Inorganic materials 0.000 claims abstract description 9
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims abstract description 9
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 24
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 22
- 239000003546 flue gas Substances 0.000 claims description 22
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 20
- 229910052717 sulfur Inorganic materials 0.000 claims description 20
- 239000011593 sulfur Substances 0.000 claims description 20
- 238000005507 spraying Methods 0.000 claims description 14
- 239000002893 slag Substances 0.000 claims description 13
- 239000012535 impurity Substances 0.000 claims description 10
- 238000005406 washing Methods 0.000 claims description 10
- 238000003825 pressing Methods 0.000 claims description 8
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 50
- 230000003647 oxidation Effects 0.000 abstract description 13
- 238000007254 oxidation reaction Methods 0.000 abstract description 13
- 239000013618 particulate matter Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 238000003723 Smelting Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 239000002608 ionic liquid Substances 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- HSYFJDYGOJKZCL-UHFFFAOYSA-L zinc;sulfite Chemical compound [Zn+2].[O-]S([O-])=O HSYFJDYGOJKZCL-UHFFFAOYSA-L 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- RQPZNWPYLFFXCP-UHFFFAOYSA-L barium dihydroxide Chemical compound [OH-].[OH-].[Ba+2] RQPZNWPYLFFXCP-UHFFFAOYSA-L 0.000 description 1
- 229910001863 barium hydroxide Inorganic materials 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000009856 non-ferrous metallurgy Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 description 1
- 229910001948 sodium oxide Inorganic materials 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 description 1
- 229960001763 zinc sulfate Drugs 0.000 description 1
- 229910000368 zinc sulfate Inorganic materials 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/025—Other waste gases from metallurgy plants
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Manufacture And Refinement Of Metals (AREA)
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Abstract
The invention provides a system and a method for treating zinc leaching residue volatilization kiln tail gas, wherein the system comprises a primary absorption chamber provided with zinc oxide powder, a secondary absorption chamber provided with zinc oxide powder and liquid alkali, an alkali absorption reaction chamber and an electric defogging reaction chamber which are sequentially connected through a pipeline; and the pipelines of the secondary absorption chamber and the alkali absorption reaction chamber are connected with an ozone generator. The tail gas of the zinc leaching residue volatilization kiln is subjected to two-step absorption and one-step alkali absorption to remove sulfur dioxide in the tail gas, then the tail gas is subjected to ozone oxidation to remove nitrogen oxides in the tail gas, then the tail gas enters the alkali absorption reaction chamber to be changed into nitrate, and particles in the tail gas are removed through the electric defogging reaction chamber, so that the tail gas emission of the zinc leaching residue volatilization kiln can meet the ultra-clean requirement.
Description
Technical Field
The invention relates to the field of tail gas treatment in non-ferrous metallurgy technology, in particular to a system and a method for treating zinc leaching residue volatilization kiln tail gas.
Background
When zinc smelting enterprises use the volatilization kiln to treat zinc leaching residues, the generated flue gas mainly comprises the following components: 10000mg/m of sulfur dioxide3Nitrogen oxides 180mg/m3100mg/m of granules3However, the fluctuation of the production process of the volatilization kiln is large, the components of the flue gas can fluctuate in a very large range, and the modes of absorbing and treating tail gas sulfur dioxide by ionic liquid, hydrogen peroxide, sodium carbonate and the like cannot reasonably use the zinc oxide powder produced by the volatilization kiln, so that the process has low degree of combination and high cost.
Some production enterprises which use zinc oxide powder to absorb sulfur dioxide are not perfect in flow and cannot meet the requirement of ultra-clean flue gas emission index, so that a method which can effectively treat the zinc leaching slag volatilization kiln tail gas is urgently needed to achieve ultra-clean emission of the tail gas.
Therefore, the prior art has defects and needs to be improved and developed.
Disclosure of Invention
In view of the defects of the prior art, the invention aims to provide a system and a method for treating zinc leaching slag volatilization kiln tail gas, and aims to solve the problem that the existing zinc leaching slag volatilization kiln tail gas cannot meet the requirement of ultra-clean flue gas emission index.
In order to solve the above technical problems, the technical solution adopted by the present invention to solve the above technical problems is as follows:
a treatment system for zinc leaching residue volatilization kiln tail gas comprises a primary absorption chamber provided with zinc oxide powder, a secondary absorption chamber provided with zinc oxide powder and liquid alkali, an alkali absorption reaction chamber and an electric defogging reaction chamber which are sequentially connected through a pipeline;
and the pipelines of the secondary absorption chamber and the alkali absorption reaction chamber are connected with an ozone generator.
The system for treating the zinc leaching residue volatilizing kiln tail gas is characterized in that an ore pulp return pipe of an inclined alkali absorption reaction chamber is arranged on the alkali absorption reaction chamber and the electric defogging reaction chamber.
The system for treating the zinc leaching residue volatilizing kiln tail gas is characterized in that a return pipe is arranged on a pipeline between the secondary absorption chamber and the alkali absorption reaction chamber and at the bottom of the electric defogging reaction chamber and is connected with a plate and frame filter press.
The system for treating the zinc leaching residue volatilizing kiln tail gas is characterized in that a pre-washing chamber is connected in front of the primary absorption chamber.
The system for treating the zinc leaching residue volatilizing kiln tail gas is characterized in that a chimney is connected behind the electric defogging reaction chamber and used for discharging the treated tail gas.
A method for treating zinc leaching residue volatilizing kiln tail gas comprises the following steps:
providing tail gas of a zinc leaching residue volatilization kiln, wherein the tail gas sequentially enters a primary absorption chamber and a secondary absorption chamber to obtain sulfur-removed tail gas;
the ozone generator generates ozone to oxidize the sulfur-removed tail gas, and then the sulfur-removed tail gas enters the alkali absorption reaction chamber to remove nitrogen oxides in the sulfur-removed tail gas to obtain nitrogen-removed tail gas;
and the denitrified tail gas enters an electric defogging reaction chamber, and particulate matters in the denitrified tail gas are removed to obtain the tail gas reaching the flue gas emission index.
The method for treating the zinc leaching residue volatilizing kiln tail gas comprises the following steps of:
enabling the tail gas to enter a primary absorption chamber, and carrying out two-stage reverse spraying absorption treatment on the tail gas by adopting zinc oxide powder to obtain a first sulfur-removal tail gas;
and the first sulfur removal tail gas enters a secondary absorption chamber, zinc oxide powder is adopted to carry out primary reverse spraying absorption treatment on the first sulfur removal tail gas, and then liquid caustic soda is adopted to react with the first sulfur removal tail gas to obtain the sulfur removal tail gas.
The method for treating the zinc leaching residue volatilizing kiln tail gas comprises the following steps of:
the ozone generator generates ozone to oxidize nitrogen oxides in the sulfur-removing tail gas into NO2Absorbing the NO in the alkali absorption reaction chamber by using liquid alkali spraying2Nitrate is generated to obtain the denitrified tail gas.
The method for treating the zinc leaching residue volatilization kiln tail gas comprises the following steps of after the tail gas is discharged from the secondary absorption chamber, before the nitrogen-removing tail gas enters the electric defogging reaction chamber and after particulate matters in the nitrogen-removing tail gas are removed:
and overflowing ore pulp carried in the second sulfur removal tail gas to a plate-and-frame filter press through a return pipe for filter pressing so as to reduce particles.
The method for treating the zinc leaching residue volatilization kiln tail gas comprises the following steps of:
and the tail gas enters a pre-washing chamber to remove solid impurities and liquid impurities in the tail gas.
Has the advantages that: the invention provides a system and a method for treating zinc leaching residue volatilization kiln tail gas, wherein the system comprises a primary absorption chamber provided with zinc oxide powder, a secondary absorption chamber provided with zinc oxide powder and liquid alkali, an alkali absorption reaction chamber and an electric defogging reaction chamber which are sequentially connected through a pipeline; and the pipelines of the secondary absorption chamber and the alkali absorption reaction chamber are connected with an ozone generator. The tail gas of the zinc leaching residue volatilization kiln is subjected to two-step absorption and one-step alkali absorption to remove sulfur dioxide in the tail gas, then the tail gas is subjected to ozone low-temperature oxidation to remove nitrogen oxide in the tail gas, then the tail gas enters an alkali absorption reaction chamber to be converted into nitrate, and three steps of ore pulp backflow, filter pressing and humidification type electric demisting are carried out to remove particles in the tail gas, so that the tail gas emission of the zinc leaching residue volatilization kiln meets the ultra-clean requirement.
Drawings
Fig. 1 is a schematic structural diagram of a zinc leaching residue volatilization kiln tail gas treatment system provided by an embodiment of the invention.
Fig. 2 is a flow chart of a zinc leaching residue volatilization kiln tail gas treatment method provided by the embodiment of the invention.
FIG. 3 is a flow chart of a process for sulfur removal from tail gas according to an embodiment of the present invention.
FIG. 4 is a flow chart of a process for nitrogen removal from tail gas according to an embodiment of the present invention.
FIG. 5 is a flow chart of a method for removing particulate matter from exhaust according to an embodiment of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer and clearer, the present invention is further described in detail below with reference to the accompanying drawings and examples. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention. It will be understood by those skilled in the art that, unless otherwise defined, all terms (including technical and scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. It will be further understood that terms, such as those defined in commonly used dictionaries, should be interpreted as having a meaning that is consistent with their meaning in the context of the prior art and will not be interpreted in an idealized or overly formal sense unless expressly so defined herein.
When zinc smelting enterprises use the volatilization kiln to treat zinc leaching residues, the generated flue gas mainly comprises the following components: 10000mg/m of sulfur dioxide3Nitrogen oxides 180mg/m3100mg/m of granules3However, as the fluctuation of the production process of the volatilization kiln is large, the components of the flue gas can fluctuate in a very large range, and the modes of absorbing and treating tail gas sulfur dioxide such as ionic liquid, hydrogen peroxide, sodium carbonate and the like cannot reasonably use the zinc oxide powder produced by the production enterprises, the process combination degree is low, the cost is high, and part of the production enterprises using the zinc oxide powder to absorb the sulfur dioxide cannot meet the requirement of ultra-clean flue gas emission indexes.
Based on the above, the invention provides a treatment system for zinc leaching residue volatilization kiln tail gas, which comprises a primary absorption chamber provided with zinc oxide powder, a secondary absorption chamber provided with zinc oxide powder and liquid alkali, an alkali absorption reaction chamber and an electric defogging reaction chamber, which are sequentially connected through a pipeline, as shown in fig. 1; and the pipelines of the secondary absorption chamber and the alkali absorption reaction chamber are connected with an ozone generator.
The tail gas of the zinc leaching residue volatilization kiln is subjected to two-step zinc oxide absorption and one-step alkali absorption to remove sulfur dioxide in the tail gas, then the tail gas is subjected to low-temperature ozone oxidation generated by an ozone generator to remove nitrogen oxide in the tail gas, then the tail gas enters an alkali absorption reaction chamber to be changed into nitrate, and particles in the tail gas are removed through wet electric demisting, so that the tail gas emission of the zinc leaching residue volatilization kiln meets the ultra-clean requirement.
Specifically, because the tail gas of the zinc leaching residue volatilization kiln contains sulfur dioxide, the sulfur dioxide in the tail gas can react with the sulfur dioxide in the tail gas to generate zinc sulfite by adding zinc oxide powder, then the zinc sulfite is changed into zinc sulfate, and then the residual sulfur dioxide in the tail gas can react with the liquid caustic soda to generate corresponding sulfite.
Preferably, the zinc oxide powder is provided by the zinc oxide powder produced by the zinc leaching residue volatilization kiln, so that raw materials can be saved, and the cost is reduced; more preferably, the zinc oxide powder can be prepared into suspension by adding water or washing liquid of the desulphurization slag returned in the process.
In some embodiments, the liquid alkali is selected from one of calcium hydroxide, sodium hydroxide and barium hydroxide, and strong alkali is selected to better absorb sulfur dioxide, so as to remove as much sulfur dioxide in the tail gas as possible. Preferably, in this embodiment, sodium hydroxide is used as the liquid alkali.
In the embodiment, a pulp return pipe which is inclined to the alkali absorption reaction chamber is arranged on the pipeline of the alkali absorption reaction chamber and the pipeline of the electric defogging reaction chamber; and return pipes are arranged on a pipeline between the secondary absorption chamber and the alkali absorption reaction chamber and at the bottom of the electric defogging reaction chamber and are connected with the plate and frame filter press.
Specifically, the tail gas of zinc leaching slag volatilization kiln is behind the secondary absorption chamber, the entrainment volume of ore pulp is big in the tail gas, consequently be in the alkali inhale the reacting chamber with be provided with the slant alkali on the pipeline of electric defogging reacting chamber and inhale the reacting chamber can make the ore pulp backward flow to the alkali inhale the reacting chamber, and the secondary absorption chamber with on the pipeline between the reacting chamber is inhaled to the alkali and the bottom of electric defogging reacting chamber also is provided with the back flow, can make sedimentary ore pulp overflow come out, further utilizes the plate frame pressure filter to carry out the filter-pressing, and the filtrating returns and uses, can reduce the flue gas particulate matter and smugglies secretly, thereby reduces particulate content in the tail gas to it smugglies the reacting chamber secretly to prevent to have the ore pulp to carry to the electric defogging reacting chamber, so that follow-up can realize the effect of electric defogging desorption particulate matter better.
In some embodiments, a pre-washing chamber is also connected before the primary absorption chamber.
Specifically, before the tail gas is treated, the tail gas can be pretreated by entering the tail gas into a pre-washing chamber, so that solid impurities and liquid impurities doped in the tail gas can be cleaned and removed, and the influence on the subsequent steps can be prevented.
Further, in some embodiments, a chimney is connected behind the electric defogging reaction chamber and used for discharging the treated tail gas.
The invention also provides a method for treating the zinc leaching residue volatilizing kiln tail gas, which comprises the following steps of:
s100, providing tail gas of a zinc leaching residue volatilization kiln, wherein the tail gas sequentially enters a primary absorption chamber and a secondary absorption chamber to obtain sulfur-removal tail gas;
s200, generating ozone by an ozone generator to oxidize the sulfur-removed tail gas, and then, removing nitrogen oxides in the sulfur-removed tail gas in an alkali absorption reaction chamber to obtain nitrogen-removed tail gas;
s300, enabling the denitrified tail gas to enter an electric defogging reaction chamber, and removing particulate matters in the denitrified tail gas to obtain the tail gas reaching the smoke emission index.
The tail gas of the zinc leaching residue volatilization kiln is subjected to two-step absorption and one-step alkali absorption to remove sulfur dioxide in the tail gas, then the tail gas is subjected to ozone low-temperature oxidation to remove nitrogen oxide in the tail gas, then the tail gas enters an alkali absorption reaction chamber to be converted into nitrate, and three steps of ore pulp backflow, filter pressing and humidification type electric demisting are carried out to remove particles in the tail gas, so that the tail gas emission of the zinc leaching residue volatilization kiln meets the ultra-clean requirement.
In this embodiment, as shown in fig. 3, the step of obtaining the sulfur-removed tail gas by sequentially entering the primary absorption chamber, the secondary absorption chamber and the alkaline absorption reaction chamber is specifically as follows:
s101, enabling the tail gas to enter a primary absorption chamber, and carrying out two-stage reverse spraying absorption treatment on the tail gas by using zinc oxide powder to obtain a first sulfur-removal tail gas;
s102, enabling the first sulfur removal tail gas to enter a secondary absorption chamber, carrying out primary reverse spraying absorption treatment on the first sulfur removal tail gas by using zinc oxide powder, and reacting liquid caustic soda with the first sulfur removal tail gas to obtain the sulfur removal tail gas.
Specifically, the sulfur dioxide in the flue gas can be removed by adopting zinc oxide powder for primary two-stage reverse spraying absorption and secondary one-stage reverse spraying absorption, more than 98.0 percent of the sulfur dioxide in the flue gas can be removed, the absorption efficiency can be greatly improved by adopting a reverse spraying absorption method, and the sulfur dioxide in the flue gas can be removed by using liquid alkali to react with the residual sulfur dioxide in the flue gas, so that the sulfur dioxide content in the finally discharged sulfur removal tail gas is lower than 0.5 percent of the sulfur dioxide content in the tail gas.
In some embodiments, as shown in fig. 4, the ozone generator generates ozone to oxidize the sulfur-removed tail gas, and then the ozone generator enters the alkaline absorption reaction chamber to remove nitrogen oxides in the sulfur-removed tail gas, so as to obtain the nitrogen-removed tail gas specifically:
the ozone generator generates ozone to oxidize nitrogen oxides in the sulfur-removing tail gas into NO2Absorbing the NO in the alkali absorption reaction chamber by using liquid alkali spraying2Nitrate is generated to obtain the denitrified tail gas.
Specifically, the sulfur-removed tail gas discharged from the secondary absorption chamber enters a pipeline, and at this time, ozone generated by an ozone generator is introduced into the pipeline, in this embodiment, a low-temperature oxidation method is preferably adopted to remove nitrogen oxides in the sulfur-removed tail gas, because more than 90% of the nitrogen oxides in the sulfur-removed tail gas are nitrogen monoxide, and the nitrogen monoxide is insoluble in water and difficult to remove, an oxidant is added, the nitrogen oxides can be oxidized at a low temperature to be oxidized into NO which is soluble in water2Then the oxidized tail gas enters an alkali absorption reaction chamber, and liquid alkali is used for spraying the oxidized tail gas to enable NO in the tail gas to be contained2And reacting with the liquid caustic soda to generate corresponding nitrate so as to obtain the nitrogen-removed tail gas, wherein more than 75% of nitrogen oxides in the tail gas can be removed through the treatment process.
In some embodiments, the temperature of the oxidation is less than 65 ℃, and the liquid base is preferably a strong sodium oxide solution.
Specifically, the ozone is prepared by an ozone generator, oxygen is converted into ozone by high-voltage discharge, the generated ozone can be directly utilized, the oxidation of the nitrogen oxides by using the ozone is realized because no catalyst is needed when the ozone oxidizes the nitrogen oxides, no heating is needed, the oxidation efficiency can reach more than 80 percent, the nitrogen oxides are irreversibly removed, no secondary pollution is generated, the excessive ozone can be decomposed in the process of spraying the liquid caustic soda, and the environmental pollution caused by the fact that the ozone is discharged along with tail gas is not needed to worry; meanwhile, the invention selects low-temperature oxidation, the temperature of the oxidation is set to be lower than 65 ℃, because the oxidation rate is higher when the temperature is lower than 65 ℃, and the best oxidation efficiency can be achieved.
In some embodiments, as shown in fig. 5, the step of removing particulate matter from the nitrogen-removed tail gas entering the electric defogging reaction chamber to obtain the tail gas reaching the flue gas emission index specifically includes:
s301, enabling the denitrified tail gas to enter an electric demisting reaction chamber, removing water vapor in the denitrified tail gas by adopting wet electric demisting, washing the electric demisting, removing particles in the denitrified tail gas, and obtaining the tail gas reaching the flue gas emission index.
Specifically, after the treatment of the preceding steps, the water vapor in the nitrogen-removed tail gas is higher, so that wet electric demisting is adopted to remove the water vapor in the nitrogen-removed tail gas, and then the electric demisting is washed by clean liquid, so that the particulate matters in the nitrogen-removed tail gas can be removed, and finally the tail gas reaching the flue gas emission index is obtained.
In some embodiments, in order to remove the particulate matters in the tail gas more fully, the method further comprises the following steps after the tail gas is discharged from the secondary absorption chamber, before the nitrogen-removed tail gas enters the electric defogging reaction chamber, and after the nitrogen-removed tail gas is removed of the particulate matters in the nitrogen-removed tail gas:
and overflowing ore pulp carried in the second sulfur removal tail gas for filter pressing so as to reduce particles.
Specifically, adopt zinc oxide powder right tail gas carries out twice back spray absorption sulfur dioxide and handles the back, the entrainment volume of ore pulp is big in the tail gas, consequently all is provided with the back flow at the export flue gas pipeline of secondary absorption room, alkali reaction chamber export flue gas pipeline and the bottom pipeline of electric defogging reaction chamber, makes sedimentary ore pulp overflow out, utilizes the filter press to carry out the filter-pressing, and the filtrating returns and uses, can reduce flue gas particulate matter and smuggle secretly to reduce the particulate matter content in the tail gas.
In some specific embodiments, after the step of providing the tail gas of the zinc leaching residue volatilization kiln, the method further comprises the steps of:
and the tail gas enters a pre-washing chamber to remove solid impurities and liquid impurities in the tail gas.
Specifically, before the tail gas is treated, the tail gas can be pretreated by entering the tail gas into a pre-washing chamber, so that solid impurities and liquid impurities doped in the tail gas can be cleaned and removed, and the influence on the subsequent steps can be prevented.
In the embodiment, the sulfur dioxide content in the finally obtained tail gas reaching the flue gas emission index is less than 50mg/m3The content of nitrogen oxide is less than 50mg/m3The content of the particles is less than 10mg/m3. The tail gas obtained by final treatment can meet the requirement of ultra-clean flue gas emission index, and cannot cause pollution to the environment.
In conclusion, the invention provides a system and a method for treating zinc leaching residue volatilization kiln tail gas, wherein the system comprises a primary absorption chamber provided with zinc oxide powder, a secondary absorption chamber provided with zinc oxide powder and liquid alkali, an alkali absorption reaction chamber and an electric defogging reaction chamber which are sequentially connected through a pipeline; and the pipelines of the secondary absorption chamber and the alkali absorption reaction chamber are connected with an ozone generator. The tail gas of the zinc leaching residue volatilization kiln is subjected to two-step absorption and one-step alkali absorption to remove sulfur dioxide in the tail gas, then the tail gas is subjected to ozone low-temperature oxidation to remove nitrogen oxide in the tail gas, then the tail gas enters an alkali absorption reaction chamber to be converted into nitrate, and three steps of ore pulp backflow, filter pressing and humidification type electric demisting are carried out to remove particles in the tail gas, so that the tail gas emission of the zinc leaching residue volatilization kiln meets the ultra-clean requirement.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. A treatment system for zinc leaching residue volatilization kiln tail gas is characterized by comprising a primary absorption chamber provided with zinc oxide powder, a secondary absorption chamber provided with zinc oxide powder and liquid alkali, an alkali absorption reaction chamber and an electric defogging reaction chamber which are sequentially connected through a pipeline;
and the pipelines of the secondary absorption chamber and the alkali absorption reaction chamber are connected with an ozone generator.
2. The system for treating the tail gas of the zinc leaching slag volatilization kiln as claimed in claim 1, wherein a pulp return pipe which is inclined to the alkali absorption reaction chamber is arranged on the pipelines of the alkali absorption reaction chamber and the electric defogging reaction chamber.
3. The system for treating the tail gas of the zinc leaching slag volatilization kiln as claimed in claim 1, wherein a return pipe is arranged on a pipeline between the secondary absorption chamber and the alkali absorption reaction chamber and at the bottom of the electric defogging reaction chamber, and the return pipe is connected with a plate and frame filter press.
4. The system for treating the tail gas of the zinc leaching slag volatilization kiln as claimed in claim 1, wherein a pre-washing chamber is connected in front of the primary absorption chamber.
5. The system for treating the tail gas of the zinc leaching slag volatilization kiln as claimed in claim 1, wherein a chimney is further connected behind the electric defogging reaction chamber and used for discharging the treated tail gas.
6. A method for treating zinc leaching residue volatilizing kiln tail gas is characterized by comprising the following steps:
providing tail gas of a zinc leaching residue volatilization kiln, wherein the tail gas sequentially enters a primary absorption chamber and a secondary absorption chamber to obtain sulfur-removed tail gas;
the ozone generator generates ozone to oxidize the sulfur-removed tail gas, and then the sulfur-removed tail gas enters the alkali absorption reaction chamber to remove nitrogen oxides in the sulfur-removed tail gas to obtain nitrogen-removed tail gas;
and the denitrified tail gas enters an electric defogging reaction chamber, and particulate matters in the denitrified tail gas are removed to obtain the tail gas reaching the flue gas emission index.
7. The method for treating the zinc leaching residue volatilization kiln tail gas as claimed in claim 6, wherein the tail gas sequentially enters the primary absorption chamber and the secondary absorption chamber, and the step of obtaining the sulfur removal tail gas comprises the following specific steps:
enabling the tail gas to enter a primary absorption chamber, and carrying out two-stage reverse spraying absorption treatment on the tail gas by adopting zinc oxide powder to obtain a first sulfur-removal tail gas;
and the first sulfur removal tail gas enters a secondary absorption chamber, zinc oxide powder is adopted to carry out primary reverse spraying absorption treatment on the first sulfur removal tail gas, and then liquid caustic soda is adopted to react with the first sulfur removal tail gas to obtain the sulfur removal tail gas.
8. The method for treating the zinc leaching slag volatilization kiln tail gas as claimed in claim 6, wherein the ozone generator generates ozone to oxidize the sulfur removal tail gas, and then the ozone is fed into the alkaline absorption reaction chamber to remove nitrogen oxides in the sulfur removal tail gas, so as to obtain the nitrogen removal tail gas, specifically comprising the following steps:
the ozone generator generates ozone to oxidize nitrogen oxides in the sulfur-removing tail gas into NO2Absorbing the NO in the alkali absorption reaction chamber by using liquid alkali spraying2Nitrate is generated to obtain the denitrified tail gas.
9. The method for treating the tail gas of the zinc leaching slag volatilization kiln as claimed in claim 7, further comprising the steps of, after the tail gas is discharged from the secondary absorption chamber, before the nitrogen-removed tail gas enters the electric defogging reaction chamber, and after the nitrogen-removed tail gas is subjected to particle removal:
and overflowing ore pulp carried in the second sulfur removal tail gas to a plate-and-frame filter press through a return pipe for filter pressing so as to reduce particles.
10. The method of processing zinc leach slag volatilization kiln tail gas according to claim 6, further comprising the step, after the step of providing the zinc leach slag volatilization kiln tail gas, of:
and the tail gas enters a pre-washing chamber to remove solid impurities and liquid impurities in the tail gas.
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Application publication date: 20211119 |