CN115011811A - Feeding joint control method for volatilization rotary kiln-desulfurization system - Google Patents
Feeding joint control method for volatilization rotary kiln-desulfurization system Download PDFInfo
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- CN115011811A CN115011811A CN202210660091.6A CN202210660091A CN115011811A CN 115011811 A CN115011811 A CN 115011811A CN 202210660091 A CN202210660091 A CN 202210660091A CN 115011811 A CN115011811 A CN 115011811A
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- 238000000034 method Methods 0.000 title claims abstract description 61
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 54
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims abstract description 84
- 229910052725 zinc Inorganic materials 0.000 claims abstract description 65
- 239000011701 zinc Substances 0.000 claims abstract description 65
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims abstract description 62
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 59
- 239000011787 zinc oxide Substances 0.000 claims abstract description 41
- 230000023556 desulfurization Effects 0.000 claims abstract description 40
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 30
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 30
- 239000011593 sulfur Substances 0.000 claims abstract description 30
- 239000000203 mixture Substances 0.000 claims abstract description 26
- 239000000463 material Substances 0.000 claims abstract description 23
- 235000011121 sodium hydroxide Nutrition 0.000 claims abstract description 19
- 238000003723 Smelting Methods 0.000 claims abstract description 17
- 239000000428 dust Substances 0.000 claims abstract description 15
- 239000000571 coke Substances 0.000 claims abstract description 14
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 14
- 239000000779 smoke Substances 0.000 claims abstract description 14
- 239000011734 sodium Substances 0.000 claims abstract description 13
- WGPCGCOKHWGKJJ-UHFFFAOYSA-N sulfanylidenezinc Chemical compound [Zn]=S WGPCGCOKHWGKJJ-UHFFFAOYSA-N 0.000 claims abstract description 13
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 12
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 12
- 238000010521 absorption reaction Methods 0.000 claims abstract description 6
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 3
- 238000009854 hydrometallurgy Methods 0.000 claims abstract description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims 1
- 238000011084 recovery Methods 0.000 abstract description 6
- 239000011268 mixed slurry Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 20
- 238000002386 leaching Methods 0.000 description 13
- 239000002893 slag Substances 0.000 description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-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 2
- 239000002253 acid Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000005083 Zinc sulfide Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000011217 control strategy Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 230000001804 emulsifying effect Effects 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000009853 pyrometallurgy Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- DRDVZXDWVBGGMH-UHFFFAOYSA-N zinc;sulfide Chemical compound [S-2].[Zn+2] DRDVZXDWVBGGMH-UHFFFAOYSA-N 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/02—Preliminary treatment of ores; Preliminary refining of zinc oxide
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B19/00—Obtaining zinc or zinc oxide
- C22B19/34—Obtaining zinc oxide
- C22B19/38—Obtaining zinc oxide in rotary furnaces
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a material feeding joint control method of a volatilization rotary kiln-desulfurization system, which comprises the steps of uniformly mixing a zinc-containing material and coke, and performing volatilization smelting in a rotary kiln to obtain zinc hypoxide smoke dust; the mixed slurry is pumped into a zinc oxide desulfurizing tower, and SO is contained at the same time 2 The tail gas of the rotary kiln is sent into a zinc oxide desulfurizing tower for absorption treatment; formation of ZnSO 3 The ore pulp is discharged and enters a zinc hydrometallurgy system for treatment, and simultaneously the desulfurized tail gas is sent to a sodium method tower for further absorbing residual SO 2 Or directly discharged outside. When the coke ratio in the mixture entering the rotary kiln is given, if the zinc-sulfur ratio in the mixture is less than 1.783, flake caustic soda is additionally added into a sodium method tower for desulfurization before the tail gas is discharged, and if the zinc-sulfur ratio in the mixture is more than 1.783, the tail gas can be directly discharged after the desulfurization of the secondary zinc oxide ore pulp. The invention realizes the optimized control of the dosage of the zinc hypoxide desulfurization and the caustic soda flake desulfurization, simplifies the zinc wet recovery process, and ensures that the standard emission of the sulfur content of the tail gas is realized by the minimum addition of the caustic soda flakeAnd the desulfurization cost can be saved.
Description
Technical Field
The invention belongs to the field of rotary kiln volatilization smelting and tail gas desulfurization of zinc-containing solid waste, and particularly relates to a feeding combined control method of a volatilization rotary kiln and a desulfurization system.
Background
The smelting of heavy metals such as zinc, lead, copper and the like mainly takes sulphide ore as a main raw material, a large amount of sulfur-containing intermediate slag materials are generated in the smelting process, for example, the sulfur content of acid leaching slag generated after the zinc sulphide ore is subjected to wet smelting is more than 6 percent, and even reaches 10 percent in individual enterprises, and the sulfur-containing intermediate materials generate a large amount of low-concentration SO in the process of comprehensive recycling in pyrometallurgy 2 Flue gas (containing SO) 2 Less than 3 percent, mostly 0.1 to 0.5 percent, and desulfurization treatment is needed before discharge to avoid environmental pollution.
For zinc smelting enterprises, the sulfur-containing acid leaching residue can be recovered in the form of zinc hypoxide smoke dust after being volatilized and smelted by a rotary kiln, and most of sulfur is SO 2 And entering the tail gas of the rotary kiln. SO in tail gas of volatilizing rotary kiln by using self-produced secondary zinc oxide smoke dust 2 Absorption (SO) 2 +ZnO=ZnSO 3 ) The method is a common means for zinc smelting enterprises to realize the standard-reaching emission of tail gas.
However, the existing method for desulfurizing tail gas by utilizing self-produced zinc hypoxide has the following defects: 1) the amount of secondary zinc oxide added is not taken into consideration. When the self-produced zinc hypoxide is sufficiently desulfurized, if the added ZnO amount is excessively higher than the required amount, the subsequent ZnSO is increased 3 The throughput of the pulp analysis process. Compared with ZnSO 3 In the ore pulp, the direct leaching of the secondary zinc oxide is easier to carry out, so that the addition of excessive unnecessary secondary zinc oxide for desulfurization is equivalent to the increase of the complexity of the process; 2) the amount of caustic soda flakes added is not considered. When the self-produced secondary zinc oxide is not enough to remove SO in the tail gas 2 In the process, a caustic soda flake desulfurization step (2NaOH + SO) is additionally added after a ZnO desulfurization procedure 2 =Na 2 SO 3 +H 2 O). When the addition amount of the caustic soda flakes is far beyond the required amount, the tail gas is ensured to be discharged after reaching the standard, the caustic soda flakes are wasted, and the desulfurization cost is increased. And blind control is carried out on the addition amount of the caustic soda flakes in order to save cost, so that the risk of over-standard emission of tail gas sulfur caused by insufficient addition amount exists. For example, Chinese patent CN201210474484.4 discloses a hypo-oxygen-containing agentThe treatment method of the zinc oxide flue gas is not described, but the regulation and control method of the addition amount of the secondary zinc oxide is not described. Chinese patent CN201310361569.6 discloses a method for realizing desulfurization of flue gas containing low-concentration sulfur dioxide by using secondary zinc oxide, and does not mention a method for controlling the addition amount of the secondary zinc oxide; chinese patent CN201520134255.7 discloses a processing system of secondary zinc oxide roasting smoke dust, which also adopts the secondary zinc oxide smoke dust to carry out desulfurization, and further adopts sodium carbonate to carry out fluorine and chlorine removal, but does not mention the control mode of the addition amount; chinese patent CN201910921186.7 discloses a flue gas desulfurization method using zinc hypoxide soot as a desulfurizing agent, which provides a way of improving desulfurization efficiency in an oxygen-enriched and foaming way, but does not consider the control strategy of the addition amount of the desulfurizing agent in each procedure; chinese patent CN201910378001.2 discloses a sulfur dioxide waste gas treatment process by a zinc oxide method, and provides a method for improving absorption efficiency by an aeration mode, but does not mention a regulation and control means of the addition amount of a desulfurizer; chinese patent CN202110064473.8 discloses a sulfur-containing waste gas desulfurization emulsion, and a preparation method and application thereof, which improves the absorption efficiency by emulsifying ore pulp, but does not mention a method for controlling the addition amount.
Therefore, a feeding joint control method for the volatilization rotary kiln-desulfurization system is urgently needed to reduce the treatment cost of enterprises and the operability of process regulation and control. Particularly, when the fluctuation of the components of the materials entering the rotary kiln is large in the smelting process of the rotary kiln, the joint control operation of the upstream and downstream processes between the rotary kiln smelting and the desulfurization system is more important, and the fluctuation of the components of the materials is always a normal state in the smelting process of the rotary kiln for treating solid wastes. In the rotary kiln smelting process with large working condition fluctuation, feeding control is carried out only by depending on experience or adjustment is carried out only by depending on an instrument, so that the difficulty of cost optimization control and the risk of over-standard tail gas sulfur emission are possibly caused.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a feeding joint control method for a volatilization rotary kiln-desulfurization system. The content of sulfur in the zinc-containing material used in the smelting process of the rotary kiln is 6-11%, the content of zinc is 11-16%, and based on the high material fluctuation range, the upstream and downstream joint control technical scheme in the smelting process is established as follows:
a feeding joint control method for a volatilization rotary kiln-desulfurization system comprises the following specific processes:
s1, the process is described, the zinc-containing material is mixed with coke, and the mixture is volatilized and smelted by a rotary kiln to obtain the secondary zinc oxide smoke dust; the secondary zinc oxide smoke dust is slurried and pumped into a zinc oxide desulfurizing tower, and SO is contained in the secondary zinc oxide smoke dust 2 The tail gas of the rotary kiln is sent into a zinc oxide desulfurizing tower for absorption treatment after passing through a washing tower; formation of ZnSO 3 The ore pulp is discharged and enters a zinc hydrometallurgy system for treatment, and simultaneously the desulfurized tail gas is sent to a sodium method tower for further absorbing residual SO 2 Or directly discharged outside.
And S2, according to the principle of feeding combined control, when the coke ratio in the mixture fed into the rotary kiln in S1 is given, if the zinc-sulfur ratio in the mixture is less than 1.783, the mixture needs to be additionally fed into a sodium method tower for desulfurization before tail gas is discharged. If the zinc-sulfur ratio in the mixture is more than 1.783, the tail gas can be directly discharged after being desulfurized by the secondary zinc oxide ore pulp; it should be noted that, based on the unit mass of the zinc oxide desulfurization capability as the calculation basis, the theoretical value of the zinc mass required by one ton of sulfur, that is, the critical value of the zinc-sulfur ratio of 1.783, can be obtained.
Further, in step S2, when the ratio of zinc to sulfur in the mixture is less than 1.783, all the generated zinc hypoxide is used for size mixing and desulfurization, and the amount of the desulfurizing caustic soda flakes additionally added to the sodium method tower is not less than the following amount: the difference between 1.97 times of the sulfur content in the mixture and 1.1 times of the zinc content in the mixture. It should be noted that the added flake caustic soda is obtained by calculation based on the desulfurization capability of flake caustic soda per unit mass, the desulfurization capability of zinc oxide per unit mass, and the zinc-sulfur ratio in the mixture.
Further, in step S2, when the ratio of zinc to sulfur in the mixture is greater than 1.783, the addition amount of the zinc hypoxide for size mixing and desulfurization is 3.12 times the sulfur content in the material. It should be noted that the added amount of zinc hypoxide is calculated based on the desulfurization capability of zinc oxide per unit mass and the zinc-sulfur ratio in the mixture. Under the condition, the self-produced zinc hypoxide has surplus, and the flake caustic soda does not need to be additionally added.
Further, the coke ratio is 0.46-0.53 in the step S2, the zinc-containing material contains 11-18% of zinc, 6-11% of sulfur and 4:1 of zinc oxide slurry mixing solid ratio in the step S1.
Further, in step S1, the rotary kiln volatilization smelting parameters are that the kiln tail pressure is 30-50 Pa, the kiln head wind pressure is 0.14-0.16 MPa, and the blast volume is 8000-8500 m 3 The rotary kiln inner diameter and length were 4.15 m and 58 m, respectively.
Further, in the step S1, the zinc content of the zinc hypoxide smoke dust is 45% -55%, and the volatilization rate of zinc is not lower than 90%.
The invention can provide technical guidance for the rotary kiln-desulfurization system feeding combined control method, and has the advantages that:
(1) the optimal control of the desulfurization amount of the zinc hypoxide is realized, and the wet recovery process of zinc is simplified. When the addition amount of the zinc hypoxide is far higher than the dosage required by desulfurization, the subsequent ZnSO can be increased 3 The processing capacity of the ore pulp analysis process. Compared with ZnSO 3 Ore pulp and direct leaching of the zinc hypoxide are easier to perform, so that adding excessive unnecessary zinc hypoxide for desulfurization is equivalent to increasing the complexity of the process.
(2) The method realizes the accurate addition and the optimized control of the desulfurizing dosage of the caustic soda flakes, ensures that the sulfur content of the tail gas reaches the standard and is discharged with the minimum addition of the caustic soda flakes, and saves the desulfurizing cost.
Drawings
FIG. 1 is a schematic view of a rotary kiln smelting-desulfurizing system for a zinc-containing material in an embodiment of the invention;
FIG. 2 is a schematic view of the feeding joint control method of the present invention.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and examples, wherein the present embodiment is based on the technical solution and provides detailed embodiments and specific operation procedures, but the scope of the present invention is not limited to the present embodiment.
All the embodiments described below provide a feeding joint control method for a volatilization rotary kiln-desulfurization system, and leaching residues of a wet zinc smelting system are mainly used as raw materials and are uniformly mixed with coke. Wherein the coke is used as fuel and reducing agent, and the zinc in the leached slag can be discharged from a kiln tail dust collecting system in the form of zinc hypoxide smoke dust after the mixture is smelted in the rotary kiln, so that the zinc in the leached slag can be used for tail gas desulfurization of the rotary kiln.
In all the following examples, the inner diameter and length of the rotary kiln are 4.15 m and 58 m, respectively, the kiln tail pressure is 30 Pa to 50 Pa, the kiln head pressure is 0.14 MPa to 0.16 MPa, and the blast volume is 8000 m 3 /h ~8500 m 3 And h, the solid-to-solid ratio of the secondary zinc oxide slurry is 4: 1.
Example 1
In the embodiment, the leaching slag contains 15 percent of zinc, 26.63 percent of water and 8.26 percent of sulfur, the adding amount of the leaching slag in one day is 383t, the adding amount of the coke powder is 180t, and the sulfur content of the coke powder is 0.49 percent. After the materials are uniformly mixed in a slag bin by a grab bucket, the materials enter a rotary kiln according to the ore feeding amount of 23.5t/h, the coke ratio in the mixture is 0.47, the zinc-sulfur ratio is 1.750, the produced secondary zinc oxide contains 45 percent of zinc, the zinc recovery rate is 90 percent, the secondary zinc oxide is completely put into a desulfurization process, simultaneously, 1.07 tons of caustic soda flakes are additionally added into a sodium method tower for desulfurization, and the tail gas SO is used for desulfurizing 2 Concentration discharge value lower than 100 mg/Nm 3 。
Example 2
In the embodiment, the leaching residue contains 17.7 percent of zinc, 27.3 percent of water and 8.08 percent of sulfur, the addition amount of the leaching residue in one day is 369t, the addition amount of the coke powder is 170t, and the sulfur content of the coke powder is 0.49 percent. After the materials are uniformly mixed in a slag bin by a grab bucket, the materials enter a rotary kiln according to the ore feeding amount of 22.5t/h, the coke ratio in the mixture is 0.46, the zinc-sulfur ratio is 2.133, the produced secondary zinc oxide contains 50 percent of Zn, the zinc recovery rate is 90 percent, the secondary zinc oxide is fed into 71 tons for desulfurization, no caustic soda flakes are additionally added, and tail gas SO is generated 2 Concentration discharge value lower than 100 mg/Nm 3 。
Example 3
In the embodiment, the leaching residue contains 11 percent of zinc, 17.97 percent of water and 6 percent of sulfur, the addition amount of the leaching residue in one day is 339t, the addition amount of the coke powder is 180t, and the sulfur content of the coke powder is 0.49 percent. After the materials are uniformly mixed in a slag bin by a grab bucket, the materials enter a rotary kiln according to the ore feeding amount of 21.6t/h, the coke ratio in the mixture is 0.53, the zinc-sulfur ratio is 1.737, the produced secondary zinc oxide contains 55 percent of Zn, the zinc recovery rate is 91 percent, the secondary zinc oxide is completely put into a sodium method tower for desulfurization, simultaneously, 1.02 tons of caustic soda flakes are additionally added into the sodium method tower for desulfurization, and the tail gas SO is used as tail gas 2 Concentration discharge value lower than 100 mg/Nm 3 。
Example 4
In the embodiment, the leaching residue contains 18 percent of zinc, 27.46 percent of water and 11 percent of sulfur, and the leaching residue is one day229t of adding amount, 120t of adding amount of coke powder and 0.40 percent of sulfur in the coke powder. After the materials are uniformly mixed in a slag bin by a grab bucket, the materials enter a rotary kiln according to the ore feeding amount of 14.5t/h, the coke ratio in the mixture is 0.52, the zinc-sulfur ratio is 1.595, the produced secondary zinc oxide contains 50 percent of Zn, the zinc recovery rate is 90 percent, the secondary zinc oxide is completely fed for desulfurization, 4.05 tons of caustic soda flakes are additionally added in a sodium method tower for desulfurization, and the tail gas SO is used for desulfurization 2 Concentration discharge value lower than 100 mg/Nm 3 。
Various corresponding changes and modifications can be made by those skilled in the art based on the above technical solutions and concepts, and all such changes and modifications should be included in the protection scope of the present invention.
Claims (6)
1. A feeding joint control method for a volatilization rotary kiln-desulfurization system is characterized by comprising the following steps: the method comprises the following steps:
s1, uniformly mixing the zinc-containing material with coke, and performing rotary kiln volatilization smelting to obtain zinc hypoxide smoke dust; the secondary zinc oxide smoke dust is slurried and pumped into a zinc oxide desulfurizing tower, and SO is contained in the secondary zinc oxide smoke dust 2 The tail gas of the rotary kiln is sent into a zinc oxide desulfurizing tower for absorption treatment after passing through a washing tower; formation of ZnSO 3 The ore pulp is discharged and enters a zinc hydrometallurgy system for treatment, and simultaneously the desulfurized tail gas is sent to a sodium method tower for further absorbing residual SO 2 Or directly discharged outside;
s2, feeding and joint control, wherein when the coke ratio of the mixture fed into the rotary kiln in S1 is given; if the zinc-sulfur ratio in the mixture is less than 1.783, adding caustic soda flakes additionally in a sodium method tower for desulfurization before discharging the tail gas; if the zinc-sulfur ratio in the mixture is more than 1.783, the tail gas can be directly discharged after the secondary zinc oxide ore pulp is desulfurized, and the desulfurizing process does not need to additionally add caustic soda flakes.
2. The feeding combined control method of the volatilization rotary kiln-desulfurization system as set forth in claim 1, wherein in step S2, when the ratio of zinc to sulfur in the mixture is less than 1.783, all the produced zinc hypoxide is used for size mixing desulfurization, and the amount of the extra desulfurized flake caustic soda added to the sodium process tower is not less than the following amount: the difference between 1.97 times of the sulfur content in the mixture and 1.1 times of the zinc content in the mixture.
3. The feeding combined control method of the volatilization rotary kiln-desulfurization system as set forth in claim 1, wherein in step S2, when the ratio of zinc to sulfur in the mixture is greater than 1.783, the addition amount of zinc hypoxide for size mixing and desulfurization is 3.12 times the sulfur content in the material.
4. The feeding combined control method for the volatilization rotary kiln-desulfurization system as set forth in claim 1, wherein the coke ratio is set to be 0.46-0.53 in step S2, the zinc-containing material contains 11-18% of zinc, 6-11% of sulfur and the slurry-solid ratio of zinc oxide is 4:1 in step S1.
5. The feeding joint control method for the volatilization rotary kiln-desulfurization system as claimed in claim 1, wherein in step S1, the volatilization smelting parameters of the rotary kiln are that the kiln tail pressure is 30 Pa-50 Pa, the kiln head wind pressure is 0.14 MPa-0.16 MPa, and the blast volume is 8000 m 3 /h ~8500 m 3 The rotary kiln inner diameter and length were 4.15 m and 58 m, respectively.
6. The volatilization rotary kiln-desulfurization system feeding combined control method as claimed in claim 1, wherein zinc in the zinc hypoxide smoke dust in step S1 is 45% -55%, and the volatilization rate of zinc is not lower than 90%.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101608266A (en) * | 2009-07-23 | 2009-12-23 | 广西冶金研究院 | A kind of cleaning collecting method and device thereof of the zinc oxide that volatilizees |
| CN103421958A (en) * | 2013-07-23 | 2013-12-04 | 湖南水口山有色金属集团有限公司 | Method for processing zinc leaching cinder through adopting oxygen enrichment and smelting for bottom blown furnace |
| CN209210894U (en) * | 2018-11-19 | 2019-08-06 | 中钢集团天澄环保科技股份有限公司 | Zinc-Bearing Wastes extract secondary zinc oxide device |
| CN110585865A (en) * | 2019-08-27 | 2019-12-20 | 昆明理工大学 | Method for treating zinc smelting sulfur dioxide flue gas by using zinc hydrometallurgy iron-containing precipitation slag |
| CN212316203U (en) * | 2020-07-23 | 2021-01-08 | 宝武集团环境资源科技有限公司 | Processing apparatus of secondary zinc oxide dust |
| CN113174496A (en) * | 2021-04-22 | 2021-07-27 | 甘肃厂坝有色金属有限责任公司 | Method and system for supplementing manganese in zinc hydrometallurgy |
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2022
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Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101608266A (en) * | 2009-07-23 | 2009-12-23 | 广西冶金研究院 | A kind of cleaning collecting method and device thereof of the zinc oxide that volatilizees |
| CN103421958A (en) * | 2013-07-23 | 2013-12-04 | 湖南水口山有色金属集团有限公司 | Method for processing zinc leaching cinder through adopting oxygen enrichment and smelting for bottom blown furnace |
| CN209210894U (en) * | 2018-11-19 | 2019-08-06 | 中钢集团天澄环保科技股份有限公司 | Zinc-Bearing Wastes extract secondary zinc oxide device |
| CN110585865A (en) * | 2019-08-27 | 2019-12-20 | 昆明理工大学 | Method for treating zinc smelting sulfur dioxide flue gas by using zinc hydrometallurgy iron-containing precipitation slag |
| CN212316203U (en) * | 2020-07-23 | 2021-01-08 | 宝武集团环境资源科技有限公司 | Processing apparatus of secondary zinc oxide dust |
| CN113174496A (en) * | 2021-04-22 | 2021-07-27 | 甘肃厂坝有色金属有限责任公司 | Method and system for supplementing manganese in zinc hydrometallurgy |
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