CN115888988B - Beneficiation method for high-sulfur high-carbon lead zinc ore under natural pH condition - Google Patents
Beneficiation method for high-sulfur high-carbon lead zinc ore under natural pH condition Download PDFInfo
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- 239000011593 sulfur Substances 0.000 title claims abstract description 126
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 126
- 238000000034 method Methods 0.000 title claims abstract description 71
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 24
- JQJCSZOEVBFDKO-UHFFFAOYSA-N lead zinc Chemical compound [Zn].[Pb] JQJCSZOEVBFDKO-UHFFFAOYSA-N 0.000 title claims abstract description 24
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims abstract description 170
- 229910052725 zinc Inorganic materials 0.000 claims abstract description 170
- 239000011701 zinc Substances 0.000 claims abstract description 170
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 111
- 239000012141 concentrate Substances 0.000 claims abstract description 75
- 230000002000 scavenging effect Effects 0.000 claims abstract description 75
- 239000003112 inhibitor Substances 0.000 claims abstract description 54
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 claims abstract description 40
- 239000012190 activator Substances 0.000 claims abstract description 36
- 229910000365 copper sulfate Inorganic materials 0.000 claims abstract description 35
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 claims abstract description 35
- WGPCGCOKHWGKJJ-UHFFFAOYSA-N sulfanylidenezinc Chemical compound [Zn]=S WGPCGCOKHWGKJJ-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000002283 diesel fuel Substances 0.000 claims abstract description 17
- 238000000227 grinding Methods 0.000 claims abstract description 15
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 239000000463 material Substances 0.000 claims abstract description 8
- 239000006260 foam Substances 0.000 claims description 52
- 239000003795 chemical substances by application Substances 0.000 claims description 34
- 238000003756 stirring Methods 0.000 claims description 33
- 229910052500 inorganic mineral Inorganic materials 0.000 claims description 24
- 239000011707 mineral Substances 0.000 claims description 24
- -1 diphenyl dithiophosphoramidate Chemical compound 0.000 claims description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 14
- 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 description 12
- 239000011734 sodium Substances 0.000 claims description 12
- 229910052708 sodium Inorganic materials 0.000 claims description 12
- 230000003213 activating effect Effects 0.000 claims description 9
- TUSDEZXZIZRFGC-UHFFFAOYSA-N 1-O-galloyl-3,6-(R)-HHDP-beta-D-glucose Natural products OC1C(O2)COC(=O)C3=CC(O)=C(O)C(O)=C3C3=C(O)C(O)=C(O)C=C3C(=O)OC1C(O)C2OC(=O)C1=CC(O)=C(O)C(O)=C1 TUSDEZXZIZRFGC-UHFFFAOYSA-N 0.000 claims description 6
- KOVPITHBHSZRLT-UHFFFAOYSA-N 2-methylpropoxymethanedithioic acid Chemical compound CC(C)COC(S)=S KOVPITHBHSZRLT-UHFFFAOYSA-N 0.000 claims description 6
- 239000001263 FEMA 3042 Substances 0.000 claims description 6
- LRBQNJMCXXYXIU-PPKXGCFTSA-N Penta-digallate-beta-D-glucose Natural products OC1=C(O)C(O)=CC(C(=O)OC=2C(=C(O)C=C(C=2)C(=O)OC[C@@H]2[C@H]([C@H](OC(=O)C=3C=C(OC(=O)C=4C=C(O)C(O)=C(O)C=4)C(O)=C(O)C=3)[C@@H](OC(=O)C=3C=C(OC(=O)C=4C=C(O)C(O)=C(O)C=4)C(O)=C(O)C=3)[C@H](OC(=O)C=3C=C(OC(=O)C=4C=C(O)C(O)=C(O)C=4)C(O)=C(O)C=3)O2)OC(=O)C=2C=C(OC(=O)C=3C=C(O)C(O)=C(O)C=3)C(O)=C(O)C=2)O)=C1 LRBQNJMCXXYXIU-PPKXGCFTSA-N 0.000 claims description 6
- CHSBUVXZAGJOFK-UHFFFAOYSA-L disodium;dioxido-bis(sulfanylidene)-$l^{6}-sulfane Chemical compound [Na+].[Na+].[O-]S([O-])(=S)=S CHSBUVXZAGJOFK-UHFFFAOYSA-L 0.000 claims description 6
- WNAHIZMDSQCWRP-UHFFFAOYSA-N dodecane-1-thiol Chemical compound CCCCCCCCCCCCS WNAHIZMDSQCWRP-UHFFFAOYSA-N 0.000 claims description 6
- CMGLSTYFWSQNEC-UHFFFAOYSA-N o-ethyl n-ethylcarbamothioate Chemical compound CCNC(=S)OCC CMGLSTYFWSQNEC-UHFFFAOYSA-N 0.000 claims description 6
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 6
- 239000001509 sodium citrate Substances 0.000 claims description 6
- NLJMYIDDQXHKNR-UHFFFAOYSA-K sodium citrate Chemical compound O.O.[Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O NLJMYIDDQXHKNR-UHFFFAOYSA-K 0.000 claims description 6
- HRZFUMHJMZEROT-UHFFFAOYSA-L sodium disulfite Chemical compound [Na+].[Na+].[O-]S(=O)S([O-])(=O)=O HRZFUMHJMZEROT-UHFFFAOYSA-L 0.000 claims description 6
- JVBXVOWTABLYPX-UHFFFAOYSA-L sodium dithionite Chemical compound [Na+].[Na+].[O-]S(=O)S([O-])=O JVBXVOWTABLYPX-UHFFFAOYSA-L 0.000 claims description 6
- 229940001584 sodium metabisulfite Drugs 0.000 claims description 6
- 235000010262 sodium metabisulphite Nutrition 0.000 claims description 6
- OJNSBQOHIIYIQN-UHFFFAOYSA-M sodium;bis(2-methylpropyl)-sulfanylidene-sulfido-$l^{5}-phosphane Chemical compound [Na+].CC(C)CP([S-])(=S)CC(C)C OJNSBQOHIIYIQN-UHFFFAOYSA-M 0.000 claims description 6
- LRBQNJMCXXYXIU-NRMVVENXSA-N tannic acid Chemical compound OC1=C(O)C(O)=CC(C(=O)OC=2C(=C(O)C=C(C=2)C(=O)OC[C@@H]2[C@H]([C@H](OC(=O)C=3C=C(OC(=O)C=4C=C(O)C(O)=C(O)C=4)C(O)=C(O)C=3)[C@@H](OC(=O)C=3C=C(OC(=O)C=4C=C(O)C(O)=C(O)C=4)C(O)=C(O)C=3)[C@@H](OC(=O)C=3C=C(OC(=O)C=4C=C(O)C(O)=C(O)C=4)C(O)=C(O)C=3)O2)OC(=O)C=2C=C(OC(=O)C=3C=C(O)C(O)=C(O)C=3)C(O)=C(O)C=2)O)=C1 LRBQNJMCXXYXIU-NRMVVENXSA-N 0.000 claims description 6
- 229940033123 tannic acid Drugs 0.000 claims description 6
- 235000015523 tannic acid Nutrition 0.000 claims description 6
- 229920002258 tannic acid Polymers 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000006080 lead scavenger Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 3
- 239000011133 lead Substances 0.000 abstract description 110
- 235000008733 Citrus aurantifolia Nutrition 0.000 abstract description 13
- 235000011941 Tilia x europaea Nutrition 0.000 abstract description 13
- 239000004571 lime Substances 0.000 abstract description 13
- 238000011084 recovery Methods 0.000 description 20
- 238000005188 flotation Methods 0.000 description 12
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 11
- 229910052683 pyrite Inorganic materials 0.000 description 11
- 239000011028 pyrite Substances 0.000 description 11
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 9
- 229910052709 silver Inorganic materials 0.000 description 9
- 239000004332 silver Substances 0.000 description 9
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 8
- 229910052737 gold Inorganic materials 0.000 description 8
- 239000010931 gold Substances 0.000 description 8
- 229910052950 sphalerite Inorganic materials 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 5
- 229910001656 zinc mineral Inorganic materials 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 229910001739 silver mineral Inorganic materials 0.000 description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 239000004088 foaming agent Substances 0.000 description 3
- 229910052949 galena Inorganic materials 0.000 description 3
- 230000005764 inhibitory process Effects 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- XCAUINMIESBTBL-UHFFFAOYSA-N lead(ii) sulfide Chemical compound [Pb]=S XCAUINMIESBTBL-UHFFFAOYSA-N 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000010408 sweeping Methods 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- PQTCMBYFWMFIGM-UHFFFAOYSA-N gold silver Chemical compound [Ag].[Au] PQTCMBYFWMFIGM-UHFFFAOYSA-N 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- BFUPQMKQJRHLRA-UHFFFAOYSA-N [Pb]=S.[Zn] Chemical compound [Pb]=S.[Zn] BFUPQMKQJRHLRA-UHFFFAOYSA-N 0.000 description 1
- XAQHXGSHRMHVMU-UHFFFAOYSA-N [S].[S] Chemical compound [S].[S] XAQHXGSHRMHVMU-UHFFFAOYSA-N 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- TUZCOAQWCRRVIP-UHFFFAOYSA-N butoxymethanedithioic acid Chemical compound CCCCOC(S)=S TUZCOAQWCRRVIP-UHFFFAOYSA-N 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 229910052952 pyrrhotite Inorganic materials 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000031068 symbiosis, encompassing mutualism through parasitism Effects 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
- 229910000368 zinc sulfate Inorganic materials 0.000 description 1
- 229960001763 zinc sulfate Drugs 0.000 description 1
- 229910052984 zinc sulfide Inorganic materials 0.000 description 1
Classifications
-
- 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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- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a beneficiation method for high-sulfur high-carbon lead zinc ore under the natural pH condition, which comprises the following steps: (1) grinding to obtain a fine material a; (2) Lead is selected, a zinc-sulfur inhibitor GY-1, diesel oil and a lead-selecting collector BP-1 are sequentially added into the fine material a, and lead concentrate b and lead-selecting tailings c are obtained through twice roughing, twice scavenging and four times selecting; (3) zinc selection: adding an iron sulfide inhibitor GY-2 and a zinc collector BP-2 into the lead dressing tailings c, and carrying out one-time roughing, three-time scavenging and three-time concentration to obtain zinc concentrate d and zinc dressing tailings e; (4) sulfur selection: adding an iron sulfide activator copper sulfate and an iron sulfide collector BP-3 into the zinc tailings e, and carrying out one-time roughing, one-time scavenging and two-time concentration to obtain sulfur concentrate f and sulfur tailings h. The invention can realize high-efficiency separation of lead, zinc and sulfur under natural pH conditions without lime.
Description
Technical Field
The invention relates to a beneficiation method, in particular to a beneficiation method for high-sulfur high-carbon lead zinc ores under the natural pH condition.
Background
Lead zinc is an important metal and is widely applied to the fields of electric industry, mechanical industry, metallurgical industry, chemical industry and the like.
The lead-zinc mineral resources in China are rich and widely distributed. However, the lead zinc ore in China has complex ore types, low grade, more associated elements and large selectivity difference, and brings great difficulty to ore dressing.
The high sulfur lead zinc ore is difficult to obtain high-grade lead and zinc concentrate because sulfur is easy to float out in the flotation process due to high sulfur element content. Therefore, most of the mineral separation methods can only adopt the traditional high-alkali mineral separation technology, the pH value of ore pulp is adjusted to be more than 12 by adding a large amount of lime, and the conventional inhibitors such as zinc sulfate, sulfite and the like are matched to fully inhibit non-target minerals, so that the separation purpose is achieved.
However, the high alkali process has the following problems: 1) The addition of a large amount of lime has an inhibition effect on associated gold and silver, and the iron sphalerite is easy to be inhibited due to the excessively high pH value in the zinc selecting process, so that the zinc recovery rate is reduced; 2) Because the pyrite is strongly inhibited by lime, the activation is difficult in the flotation process, a large amount of sulfuric acid needs to be added, and the recovery rate of sulfur concentrate is low; 3) Excessive lime causes scaling of a flotation pipeline to be easy to block; 4) The pH value of the tailing pulp is high, the COD content is high, the heavy metal ion content is high, the wastewater treatment cost is high, and the environmental protection risk pressure is greatly increased.
How to overcome the defects of the existing high-alkali mineral separation technology, and to find a novel method for efficiently separating lead, zinc and sulfur from high-sulfur lead and zinc ores under the natural pH condition without lime, which is a technical problem which needs to be solved in the field.
Disclosure of Invention
The invention aims to solve the technical problem of providing a beneficiation method for high-sulfur high-carbon lead-zinc ore under the natural pH condition, so that lead-zinc-sulfur can be efficiently separated under the natural pH condition without lime.
In order to solve the technical problems, the beneficiation method for the high-sulfur high-carbon lead zinc ore under the natural pH condition comprises the following steps:
(1) Grinding, namely crushing and grinding raw ores until-74 um accounts for 70-85%, and adding water to adjust the raw ores to pulp with solid content of 30-40% to obtain a fine material a;
(2) Under the condition of natural pH, zinc-sulfur inhibitor GY-1, diesel oil and lead-selecting collector BP-1 are sequentially added into the fine material a, and lead concentrate b and lead-selecting tailings c are obtained through twice rough concentration, twice scavenging and four times concentration;
(3) Zinc selection: under the condition of natural pH, adding an iron sulfide inhibitor GY-2, a zinc activator copper sulfate and a zinc collector BP-2 into the lead tailings c, and carrying out one-time roughing, three-time scavenging and three-time concentration to obtain zinc concentrate d and zinc tailings e;
(4) Sulfur selection: under the condition of natural pH, adding an iron sulfide activator copper sulfate and an iron sulfide collector BP-3 into the zinc tailings e, and carrying out one-time roughing, one-time scavenging and two-time concentration to obtain sulfur concentrate f and sulfur tailings h.
In the step (2), the second lead roughing foam is added with diesel oil and stirred for first-stage concentration, the first-stage concentration foam is added with zinc-sulfur inhibitor GY-1 and lead collector BP-1 and stirred for second-stage concentration, the second-stage concentration foam and the first lead roughing foam are combined and stirred for third-stage concentration, the third-stage concentration foam is stirred for fourth-stage concentration, the fourth-stage concentration foam is lead concentrate, the concentrated middlings are sequentially returned, the first lead roughing middlings are added with lead collector BP-1 and stirred for second lead roughing operation, the second lead roughing middlings are combined with lead scavenger and stirred for first-stage scavenging operation, the first middlings are stirred for second-stage scavenging operation, and the first scavenging foams are sequentially returned to the previous operation respectively; the technological conditions of the lead roughing 1 are that 200-550g/t of inhibitor is added, stirring is carried out for 3-4 minutes, then 15-30g/t of carbon collector diesel oil and 120-240g/t of lead collector are added, and stirring is carried out for 2-3 minutes; the technological conditions of the lead roughing 2 are that a lead collecting agent is added for 10-30g/t and stirred for 2-3 minutes; the technological condition of the lead scavenging is that a lead collecting agent is added for 5-20g/t; adding 5-10g/t of carbon collector diesel under the process condition of lead carefully selecting 1; the technological condition of lead concentration 2 is that zinc-sulfur inhibitor 50-200g/t and lead collector 10-20g/t are added.
In the step (2), the zinc-sulfur inhibitor GY-1 consists of sodium tannic acid, sodium humate and sodium dithiosulfate, wherein the mass ratio of the sodium tannic acid to the sodium humate to the sodium dithiosulfate is 4-8:2-5:2-6.
In the step (2), the lead collector BP-1 consists of diphenyl dithiophosphoramidate, sodium diisobutyl dithiophosphinate and dodecyl mercaptan, wherein the mass ratio of the diphenyl dithiophosphoramidate to the sodium diisobutyl dithiophosphinate to the dodecyl mercaptan is (1-6): 1-4:3-6.
In the step (3), the zinc roughing foam is added with the iron sulfide inhibitor and stirred for first-stage concentration, the first-stage concentration foam is added with the iron sulfide inhibitor and stirred for second-stage concentration, the second-stage concentration foam is stirred for third-stage concentration, and the three-stage concentration concentrate is zinc concentrate; adding a zinc activating agent and a zinc collecting agent into the zinc roughing middlings, performing first-stage scavenging, adding the zinc activating agent and the zinc collecting agent in the first-stage scavenging, stirring the zinc activating agent and the zinc collecting agent, performing second-stage scavenging, stirring the second-stage scavenging middlings, performing third-stage scavenging, and sequentially returning scavenging foam to the previous operation to obtain zinc tailings e; 200-600g/t of iron sulfide inhibitor is added in the rough zinc concentration, 300-700g/t of copper sulfate is used as a zinc activator, 20-80g/t of zinc collector is used, the process condition of zinc concentration 1 is that 100-350g/t of iron sulfide inhibitor is added, the second-stage concentration is carried out after stirring, the process condition of zinc concentration 2 is that 50-250g/t of iron sulfide inhibitor is added, 2-5g/t of zinc collector is used, the three-stage concentration is carried out after stirring, and the three-stage concentrate is zinc concentrate; the process conditions of the zinc scavenging 1 are that 20-80g/t of zinc activator copper sulfate is added, 2-5g/t of zinc collecting agent is added, the process conditions of the zinc scavenging 2 are that 20-50g/t of zinc activator copper sulfate is added, 1-4g/t of zinc collecting agent is added, scavenging foam is returned to the previous operation in sequence, and tailings enter the next sulfur-selecting operation.
In the step (3), the iron sulfide inhibitor GY-2 consists of sodium metabisulfite, sodium dithionite and sodium citrate, wherein the mass ratio of the sodium metabisulfite to the sodium dithionite to the sodium citrate is 3-8:1-3:1-6.
In the step (3), the zinc collector BP-2 consists of ethyl thiourethane and ethyl thionitrogen acrylonitrile ester, wherein the mass ratio of the ethyl thiourethane to the ethyl thionitrogen acrylonitrile ester is 1-8:9-2.
In the step (4), the sulfur roughing foam is added with a collector and stirred for first-stage concentration, and the first-stage concentration foam is stirred for second-stage concentration, wherein the second-stage concentration concentrate is sulfur concentrate; adding a sulfur activator and a sulfur collector into the sulfur roughing middlings, performing first-stage scavenging, and returning scavenging foam to the sulfur roughing operation sequentially to obtain sulfur tailings h; 50-120g/t of copper sulfate as an iron sulfide activator is added in the rough concentration of sulfur, 100-200g/t of sulfur collector is added in the rough concentration of sulfur, the technological conditions of sulfur concentration 1 are that 5-10g/t of iron sulfide collector is added in the rough concentration of sulfur, and the secondary concentration is carried out after stirring, wherein the secondary concentrate is sulfur concentrate; the process conditions of the zinc scavenging 1 are that 10-30g/t of copper sulfate as a sulfur activator and 10-20g/t of a sulfur collector are added, scavenging foam is sequentially returned to sulfur roughing operation, and the sulfur tailings are the final tailings.
In the step (4), the sulfur collector BP-3 consists of isobutyl xanthate and isopentyl xanthate propylene ester, wherein the mass ratio of the isobutyl xanthate to the isopentyl xanthate propylene ester is 2-7:8-3.
The pH value is 6-8.
According to the method, in order to realize that lead, zinc and sulfur can be separated efficiently under the natural pH condition without lime, the invention is matched with the zinc and pyrite formula inhibitor, so that the sulfur minerals are effectively inhibited by the high-sulfur high-carbon lead-zinc ore under the natural pH condition, the difficult problems that the lead-sulfur minerals of the high-sulfur lead-zinc ore can be separated effectively and the zinc-sulfur of the high-sulfur lead-zinc ore can be separated effectively only by lime are solved, and better lead, zinc and sulfur concentrate grades and recovery rates are obtained. The grade of the lead concentrate can reach above 63.36 percent, and the lead recovery rate can reach above 90.76 percent; the grade of zinc concentrate is improved to more than 46% from 45%, and the zinc recovery rate is improved to more than 94% from 92%; the grade of the sulfur concentrate is improved from 39% to 46.5%, and the recovery rate of sulfur operation is improved from 45% to 76.34%. The beneficiation reagent is clean and environment-friendly, the COD content of the tail water after flotation is lower than that of the national standard, the wastewater treatment cost is effectively reduced, and the wastewater recycling rate is improved.
The beneficiation method has the following technical innovation and characteristics:
(1) The invention eliminates the need of adding a large amount of lime in the conventional lead-zinc flotation of the high-sulfur lead-zinc ore, and saves the cost of lime preparation, manual pumping, sand pumping and the like;
(2) The pH value of the flotation ore pulp is 6-8, the natural pH range of the ore pulp is adopted, the inhibitor dosage is small, the inhibition effect on associated gold and silver noble metals is weak, and the recovery rate of associated gold and silver minerals in lead concentrate is effectively improved;
(3) According to the invention, the carbon minerals are collected by adding the diesel oil through lead separation operation, the adsorption of carbon to the medicament is reduced, the dosage of the lead collecting agent is saved, the lead is carefully selected, the diesel oil is added to prevent the carbonaceous adsorbing agent from rushing to float, the lead minerals fall off the groove, and better lead mineral separation technical indexes are obtained;
(4) The lead flotation collector BP-1 has good selectivity on lead minerals in the lead separation process, almost has no collecting effect on zinc minerals and pyrite minerals, is suitable for high-efficiency separation of lead and zinc-sulfur minerals, is added with diesel oil as a carbon collector, and enriches carbon into lead concentrate together, so that the consumption of the lead separation collector can be reduced, and the mineral separation technical index can be improved;
(5) The zinc flotation collector BP-2 has a special separation effect on zinc minerals, has extremely weak collection performance on pyrite, is beneficial to zinc-sulfur separation, and can obtain high-quality zinc concentrate, under the condition of natural pH value, excessive inhibition of a large amount of lime is avoided, the floatability of the zinc blende and part of refractory silver minerals is obviously improved, and particularly, the enrichment of silver minerals in the zinc concentrate is obviously increased;
(6) According to the invention, through the medicament proportion, the high-efficiency collecting medicament for the pyrite which replaces the butyl xanthate is invented, and the beneficiation wastewater is returned for recycling without influencing the technical index of lead and zinc beneficiation;
(7) The COD content of the flotation tail water is less than 40ml/L, the heavy metal ion content is low, the flotation tail water does not need to treat COD, the wastewater treatment cost is obviously reduced, and the mine environmental protection level is essentially improved;
(8) The flotation operation is simpler and more stable and is easy to control, and the pH value change caused by fluctuation of lime quality, insufficient supply and the like can not be caused, so that the flotation operation index is greatly fluctuated.
Drawings
FIG. 1 is a process flow diagram of the method of the present invention;
FIG. 2 is a molecular structural diagram of a lead collector BP-1;
FIG. 3 is a molecular structural diagram of a zinc collector BP-2;
FIG. 4 is a molecular structural diagram of the sulfur collector BP-3.
Detailed Description
The invention is described in detail below in connection with specific embodiments:
as shown in fig. 1, the beneficiation method for the high-sulfur high-carbon lead zinc ore under the natural pH condition comprises the following steps:
(1) Grinding, namely crushing and grinding raw ores until-74 um accounts for 70-85%, and adding water to adjust the raw ores to pulp with solid content of 30-40% to obtain a fine material a;
(2) Under the condition of natural pH, zinc-sulfur inhibitor GY-1, diesel oil and lead-selecting collector BP-1 are sequentially added into the fine material a, and lead concentrate b and lead-selecting tailings c are obtained through twice rough concentration, twice scavenging and four times concentration;
(3) Zinc selection: under the condition of natural pH, adding an iron sulfide inhibitor GY-2, a zinc activator copper sulfate and a zinc collector BP-2 into the lead tailings c, and carrying out one-time roughing, three-time scavenging and three-time concentration to obtain zinc concentrate d and zinc tailings e;
(4) Sulfur selection: under the condition of natural pH, adding an iron sulfide activator copper sulfate and an iron sulfide collector BP-3 into the zinc tailings e, and carrying out one-time roughing, one-time scavenging and two-time concentration to obtain sulfur concentrate f and sulfur tailings h.
In the step (2), the second lead roughing foam is added with diesel oil and stirred for first-stage concentration, the first-stage concentration foam is added with zinc-sulfur inhibitor GY-1 and lead collector BP-1 and stirred for second-stage concentration, the second-stage concentration foam and the first lead roughing foam are combined and stirred for third-stage concentration, the third-stage concentration foam is stirred for fourth-stage concentration, the fourth-stage concentration foam is lead concentrate, the concentrated middlings are sequentially returned, the first lead roughing middlings are added with lead collector BP-1 and stirred for second lead roughing operation, the second lead roughing middlings are combined with lead scavenger and stirred for first-stage scavenging operation, the first middlings are stirred for second-stage scavenging operation, and the first scavenging foams are sequentially returned to the previous operation respectively; the technological conditions of the lead roughing 1 are that 200-550g/t of inhibitor is added, stirring is carried out for 3-4 minutes, then 15-30g/t of carbon collector diesel oil and 120-240g/t of lead collector are added, and stirring is carried out for 2-3 minutes; the technological conditions of the lead roughing 2 are that a lead collecting agent is added for 10-30g/t and stirred for 2-3 minutes; the technological condition of the lead scavenging is that a lead collecting agent is added for 5-20g/t; adding 5-10g/t of carbon collector diesel under the process condition of lead carefully selecting 1; the technological condition of lead concentration 2 is that zinc-sulfur inhibitor 50-200g/t and lead collector 10-20g/t are added.
In the step (2), the zinc-sulfur inhibitor GY-1 consists of sodium tannic acid, sodium humate and sodium dithiosulfate, wherein the mass ratio of the sodium tannic acid to the sodium humate to the sodium dithiosulfate is 4-8:2-5:2-6.
In the step (2), the lead collector BP-1 consists of diphenyl dithiophosphoramidate, sodium diisobutyl dithiophosphinate and dodecyl mercaptan, wherein the mass ratio of the diphenyl dithiophosphoramidate to the sodium diisobutyl dithiophosphinate to the dodecyl mercaptan is (1-6): 1-4:3-6.
In the step (3), the zinc roughing foam is added with the iron sulfide inhibitor and stirred for first-stage concentration, the first-stage concentration foam is added with the iron sulfide inhibitor and stirred for second-stage concentration, the second-stage concentration foam is stirred for third-stage concentration, and the three-stage concentration concentrate is zinc concentrate; adding a zinc activating agent and a zinc collecting agent into the zinc roughing middlings, performing first-stage scavenging, adding the zinc activating agent and the zinc collecting agent in the first-stage scavenging, stirring the zinc activating agent and the zinc collecting agent, performing second-stage scavenging, stirring the second-stage scavenging middlings, performing third-stage scavenging, and sequentially returning scavenging foam to the previous operation to obtain zinc tailings e; 200-600g/t of iron sulfide inhibitor is added in the rough zinc concentration, 300-700g/t of copper sulfate is used as a zinc activator, 20-80g/t of zinc collector is used, the process condition of zinc concentration 1 is that 100-350g/t of iron sulfide inhibitor is added, the second-stage concentration is carried out after stirring, the process condition of zinc concentration 2 is that 50-250g/t of iron sulfide inhibitor is added, 2-5g/t of zinc collector is used, the three-stage concentration is carried out after stirring, and the three-stage concentrate is zinc concentrate; the process conditions of the zinc scavenging 1 are that 20-80g/t of zinc activator copper sulfate is added, 2-5g/t of zinc collecting agent is added, the process conditions of the zinc scavenging 2 are that 20-50g/t of zinc activator copper sulfate is added, 1-4g/t of zinc collecting agent is added, scavenging foam is returned to the previous operation in sequence, and tailings enter the next sulfur-selecting operation.
In the step (3), the iron sulfide inhibitor GY-2 consists of sodium metabisulfite, sodium dithionite and sodium citrate, wherein the mass ratio of the sodium metabisulfite to the sodium dithionite to the sodium citrate is 3-8:1-3:1-6.
In the step (3), the zinc collector BP-2 consists of ethyl thiourethane and ethyl thionitrogen acrylonitrile ester, wherein the mass ratio of the ethyl thiourethane to the ethyl thionitrogen acrylonitrile ester is 1-8:9-2.
In the step (4), the sulfur roughing foam is added with a collector and stirred for first-stage concentration, and the first-stage concentration foam is stirred for second-stage concentration, wherein the second-stage concentration concentrate is sulfur concentrate; adding a sulfur activator and a sulfur collector into the sulfur roughing middlings, performing first-stage scavenging, and returning scavenging foam to the sulfur roughing operation sequentially to obtain sulfur tailings h; 50-120g/t of copper sulfate as an iron sulfide activator is added in the rough concentration of sulfur, 100-200g/t of sulfur collector is added in the rough concentration of sulfur, the technological conditions of sulfur concentration 1 are that 5-10g/t of iron sulfide collector is added in the rough concentration of sulfur, and the secondary concentration is carried out after stirring, wherein the secondary concentrate is sulfur concentrate; the process conditions of the zinc scavenging 1 are that 10-30g/t of copper sulfate as a sulfur activator and 10-20g/t of a sulfur collector are added, scavenging foam is sequentially returned to sulfur roughing operation, and the sulfur tailings are the final tailings.
In the step (4), the sulfur collector BP-3 consists of isobutyl xanthate and isopentyl xanthate propylene ester, wherein the mass ratio of the isobutyl xanthate to the isopentyl xanthate propylene ester is 2-7:8-3.
In the process of the invention, the pH is from 6 to 8, i.e.at natural pH.
Example 1
Some lead-zinc concentrating mill in Hunan, the crude ore contains 2.43% of lead, 6.50% of zinc, 20.56% of sulfur, 70g/t of silver and 4.03% of carbon; the main metal minerals are sulphide minerals such as pyrite, pyrrhotite, marmatite, galena and the like, the floatability of the lead minerals is good, zinc is high-iron marmatite because the iron content reaches 16%, the floatability is poor, the embedding granularity of the sulphur minerals is coarse, the floatability is good, and the ore sample is processed by the following process steps:
A. grinding: grinding raw ore to obtain fine powder with fineness of-74 um and content of 72%;
B. Lead is preferably selected: the process conditions for the lead roughing 1 are as follows: adding 500g/t of zinc-sulfur inhibitor, stirring for 3-4 min, then adding 20g/t of carbon collector diesel oil and 160g/t of lead collector, stirring for 2-3 min, wherein the process condition of the preferential lead roughing 2 is that the lead collector is added for 20g/t, and stirring for 2-3 min; the process condition of the preferential lead scavenger 1 is that a lead collector is added by 10g/t; adding 5g/t of carbon collector diesel oil under the process conditions of lead selection 1; the process conditions of the preferential lead selection 2 are that zinc-sulfur inhibitor 100g/t and lead collector 10g/t are added;
C. Zinc is preferably selected: the method comprises the steps of (1) selecting zinc and zinc roughing, adding 450g/t of sulfur inhibitor, 550g/t of zinc activator copper sulfate and 45g/t of zinc collector, selecting zinc 1 preferably, stirring 200g/t of sulfur inhibitor, performing secondary selection, selecting zinc 2 preferably, adding 50g/t of sulfur inhibitor and 2g/t of zinc collector, stirring, performing three-stage selection, and obtaining zinc concentrate as three-stage concentrate; the process conditions of the preferential selection of the zinc scavenging 1 are 50g/t of copper sulfate serving as a zinc activator and 3g/t of zinc collecting agent, the process conditions of the preferential selection of the zinc scavenging 2 are 20g/t of copper sulfate serving as a zinc activator and 2g/t of zinc collecting agent, and the scavenging foam sequentially returns to the previous operation;
D. Sulfur is preferably selected: adding 100g/t of copper sulfate serving as an iron sulfide activator and 100g/t of a sulfur collector in the prior sulfur-sulfur roughing, and carrying out secondary concentration after stirring under the process condition that 5g/t of the iron sulfide collector is added in the prior sulfur-concentration 1, wherein secondary concentrate is sulfur concentrate; the process condition of the preferential zinc scavenging 1 is that 15g/t of copper sulfate as a sulfur activator and 10g/t of sulfur collector are added, the scavenging foam is sequentially returned to the sulfur roughing operation, and the sulfur tailings are the final tailings.
By adopting the process to treat the high-sulfur lead zinc ore, lead concentrate containing 63.36% of lead and 90.76% of lead recovery rate can be obtained, the recovery rate of silver in the lead concentrate is 47.28%, zinc content is 46.55%, zinc recovery rate is 94.67% of zinc concentrate, sulfur concentrate grade is 46.5%, and sulfur operation recovery rate is 76.34%; compared with the high-alkali process, the silver recovery rate in the lead concentrate is improved by 4.46 percent, the grade of the zinc concentrate is improved to over 46 percent from 45 percent, the zinc recovery rate is improved to over 94 percent from 92 percent, the grade of the sulfur concentrate is improved to 46.5 percent from 39 percent, the sulfur operation recovery rate is improved to 76.34 percent from 45 percent, and the comprehensive utilization rate of mineral resources is obviously improved.
Example two
A certain lead-zinc concentrating plant in inner Mongolia, wherein the raw ore contains 4.20 percent of lead, 3.50 percent of zinc, 10.30 percent of sulfur, 120g/t of silver and 2g/t of gold; the main metal minerals are sulphide minerals such as pyrite, sphalerite and galena, the lead-zinc minerals are not oxidized, the embedded granularity is medium and coarse, the floatability is good, and the ore sample is processed by the following process steps:
A. Grinding: grinding raw ore to obtain fine powder with fineness of-74 um content of 75%;
B. Lead is preferably selected: the process conditions for lead roughing are as follows: adding 200g/t of zinc-sulfur inhibitor, stirring for 3-4 minutes, then adding 220g/t of lead collector, stirring for 2-3 minutes, wherein the process condition of selecting lead to sweep is that adding 10g/t of lead collector; adding 5g/t of lead collector under the process conditions of selecting lead second and sweeping; the process conditions of the preferential lead selection 2 are that zinc-sulfur inhibitor 100g/t and lead collector 5g/t are added;
C. Zinc is preferably selected: preferably selecting zinc and coarse dressing, adding 300g/t of sulfur inhibitor, 350g/t of zinc activator copper sulfate, 30g/t of zinc collector and 10g/t of foaming agent, wherein the technological conditions of selecting zinc and fine dressing 1 are that 100g/t of sulfur inhibitor is added, stirring and then three-stage fine dressing are carried out, and three-stage concentrate is zinc concentrate; the process conditions of the preferential zinc scavenging 1 are 20g/t of adding zinc activator copper sulfate and 2g/t of zinc collector, the process conditions of the preferential zinc scavenging 2 are 10g/t of adding zinc activator copper sulfate and 2g/t of zinc collector, scavenging foam is sequentially returned to the previous operation, and tailings enter the next sulfur-selecting operation.
D. Sulfur is preferably selected: because the raw ore contains gold, the part Jin Qianbu is fine in granularity, and is closely intergrown with pyrite, the ore grinding is difficult to be dissociated, 200g/t of copper sulfate is added in the rough concentration of sulfur selection, 80g/t of sulfur selection collector, 30g/t of foaming agent, 10g/t of sulfur scavenging collector and 5g/t of foaming agent are added in the rough concentration of sulfur selection; sulfur concentration is carried out in two stages without adding any reagent, and the concentrate is gold-containing sulfur concentrate.
By adopting the process to treat the gold-silver-containing lead-zinc ore, lead concentrate containing lead 70.28% and lead recovery 92.56% can be obtained, the lead concentrate contains 36g/t of gold, 38.26% of gold recovery, 1258g/t of silver, 79.28% of silver recovery, 57.52% of zinc and 93.26% of zinc concentrate, the lead-zinc ore dressing technical index is obviously improved, and the comprehensive utilization rate of associated gold-silver mineral resources is improved.
Example III
1.86 Percent of lead and zinc ore dressing plant in Hunan, 7.19 percent of zinc, 32.69 percent of sulfur, 6g/t of silver and 5.43 percent of carbon are contained in raw ore; the main metal minerals are sulphide minerals such as pyrite, sphalerite and galena, the lead oxidation rate of the lead-zinc minerals is 14.38%, the zinc oxidation rate is 6.75%, the lead embedding granularity is very fine, the grain diameter is mainly between 0.005 and 0.046mm, complex symbiosis with pyrite and sphalerite is difficult to dissociate, the grain diameter of sphalerite is mainly between 0.02 and 0.18mm, and the sphalerite is usually continuous with pyrite and gangue; the ore sample is processed by the following process steps:
A. grinding: grinding raw ore into fine powder and mixing pulp, wherein the grinding fineness is that the content of-74 um accounts for 85 percent;
B. Lead is preferably selected: the process conditions for lead roughing are as follows: adding 400g/t of zinc-sulfur inhibitor, stirring for 3-4 minutes, then adding 30g/t of diesel oil and 160g/t of lead collector, stirring for 2-3 minutes, wherein the process condition of preferentially selecting lead to sweep is that adding 10g/t of lead collector; adding 5g/t of lead collector under the process conditions of selecting lead second and sweeping; the technological conditions of the preferential lead selection 2 are that zinc-sulfur inhibitor 100g/t, lead collector 5g/t and diesel oil 5g/t are added;
C. Zinc is preferably selected: preferably selecting zinc, coarsely selecting and adding 400g/t of iron sulfide inhibitor, 600g/t of zinc activator copper sulfate and 80g/t of zinc collector, wherein the process condition of selecting zinc and selecting 1 is that adding 100g/t of iron sulfide inhibitor, stirring and then carrying out three-stage selection, wherein three-stage concentrate is zinc concentrate; the process conditions of the preferential zinc scavenging 1 are 50g/t of adding zinc activator copper sulfate and 5g/t of zinc collector, the process conditions of the preferential zinc scavenging 2 are 20g/t of adding zinc activator copper sulfate and 2g/t of zinc collector, scavenging foam is sequentially returned to the previous operation, and tailings enter the next sulfur-selecting operation.
D. sulfur is preferably selected: adding 100g/t of copper sulfate into the sulfur-selecting roughing process, 100g/t of sulfur-selecting collector, and 20g/t of sulfur-selecting collector into the sulfur-sweeping process; sulfur concentration is carried out in two stages without adding any reagent, and the concentrate is the sulfur concentrate.
The high-sulfur high-carbon lead-zinc ore is treated by the process, lead concentrate containing 40.68% of lead and 54.32% of lead recovery rate, zinc concentrate containing 48.52% of zinc and 88.26% of zinc recovery rate, sulfur concentrate containing 48.65% of sulfur and sulfur recovery rate of 86.75% of sulfur concentrate can be obtained, and valuable minerals in ore resources are efficiently recovered.
Claims (5)
1. A mineral separation method of high-sulfur high-carbon lead zinc ore under the natural pH condition is characterized by comprising the following steps:
(1) Grinding, namely crushing and grinding raw ores until-74 um accounts for 70-85%, and adding water to adjust the raw ores to pulp with solid content of 30-40% to obtain a fine material a;
(2) Under the condition of natural pH, zinc-sulfur inhibitor GY-1, diesel oil and lead-selecting collector BP-1 are sequentially added into the fine material a, and lead concentrate b and lead-selecting tailings c are obtained through twice rough concentration, twice scavenging and four times concentration;
(3) Zinc selection: under the condition of natural pH, adding an iron sulfide inhibitor GY-2, a zinc activator copper sulfate and a zinc collector BP-2 into the lead tailings c, and carrying out one-time roughing, three-time scavenging and three-time concentration to obtain zinc concentrate d and zinc tailings e;
(4) Sulfur selection: under the condition of natural pH, adding an iron sulfide activator copper sulfate and an iron sulfide collector BP-3 into the zinc tailings e, and carrying out primary roughing, primary scavenging and secondary concentration to obtain sulfur concentrate f and sulfur tailings h;
in the step (2), the lead collector BP-1 consists of diphenyl dithiophosphoramidate, sodium diisobutyl dithiophosphinate and dodecyl mercaptan, wherein the mass ratio of the diphenyl dithiophosphoramidate to the sodium diisobutyl dithiophosphinate to the dodecyl mercaptan is (1-6): 1-4:3-6;
In the step (3), the zinc collector BP-2 consists of ethyl thiourethane and ethyl thionitrogen acrylonitrile ester, wherein the mass ratio of the ethyl thiourethane to the ethyl thionitrogen acrylonitrile ester is 1-8:9-2;
in the step (4), the sulfur collector BP-3 consists of isobutyl xanthate and isopentyl xanthate propylene ester, wherein the mass ratio of the isobutyl xanthate to the isopentyl xanthate propylene ester is 2-7:8-3;
In the step (2), the zinc-sulfur inhibitor GY-1 consists of sodium tannic acid, sodium humate and sodium dithiosulfate, wherein the mass ratio of the sodium tannic acid to the sodium humate to the sodium dithiosulfate is 4-8:2-5:2-6;
In the step (3), the iron sulfide inhibitor GY-2 consists of sodium metabisulfite, sodium dithionite and sodium citrate, wherein the mass ratio of the sodium metabisulfite to the sodium dithionite to the sodium citrate is 3-8:1-3:1-6.
2. The method according to claim 1, wherein: in the step (2), the second lead roughing foam is added with diesel oil and stirred for first-stage concentration, the first-stage concentration foam is added with zinc-sulfur inhibitor GY-1 and lead collector BP-1 and stirred for second-stage concentration, the second-stage concentration foam and the first lead roughing foam are combined and stirred for third-stage concentration, the third-stage concentration foam is stirred for fourth-stage concentration, the fourth-stage concentration foam is lead concentrate, the concentrated middlings are sequentially returned, the first lead roughing middlings are added with lead collector BP-1 and stirred for second lead roughing operation, the second lead roughing middlings are combined with lead scavenger and stirred for first-stage scavenging operation, the first middlings are stirred for second-stage scavenging operation, and the first scavenging foams are sequentially returned to the previous operation respectively; the technological conditions of the lead roughing 1 are that 200-550g/t of inhibitor is added, stirring is carried out for 3-4 minutes, then 15-30g/t of carbon collector diesel oil and 120-240g/t of lead collector are added, and stirring is carried out for 2-3 minutes; the technological conditions of the lead roughing 2 are that a lead collecting agent is added for 10-30g/t and stirred for 2-3 minutes; the technological condition of the lead scavenging is that a lead collecting agent is added for 5-20g/t; adding 5-10g/t of carbon collector diesel under the process condition of lead carefully selecting 1; the technological condition of lead concentration 2 is that zinc-sulfur inhibitor 50-200g/t and lead collector 10-20g/t are added.
3. The method according to claim 1, wherein: in the step (3), the zinc roughing foam is added with the iron sulfide inhibitor and stirred for first-stage concentration, the first-stage concentration foam is added with the iron sulfide inhibitor and stirred for second-stage concentration, the second-stage concentration foam is stirred for third-stage concentration, and the three-stage concentration concentrate is zinc concentrate; adding a zinc activating agent and a zinc collecting agent into the zinc roughing middlings, performing first-stage scavenging, adding the zinc activating agent and the zinc collecting agent in the first-stage scavenging, stirring the zinc activating agent and the zinc collecting agent, performing second-stage scavenging, stirring the second-stage scavenging middlings, performing third-stage scavenging, and sequentially returning scavenging foam to the previous operation to obtain zinc tailings e; 200-600g/t of iron sulfide inhibitor is added in the rough zinc concentration, 300-700g/t of copper sulfate is used as a zinc activator, 20-80g/t of zinc collector is used, the process condition of zinc concentration 1 is that 100-350g/t of iron sulfide inhibitor is added, the second-stage concentration is carried out after stirring, the process condition of zinc concentration 2 is that 50-250g/t of iron sulfide inhibitor is added, 2-5g/t of zinc collector is used, the three-stage concentration is carried out after stirring, and the three-stage concentrate is zinc concentrate; the process conditions of the zinc scavenging 1 are that 20-80g/t of zinc activator copper sulfate is added, 2-5g/t of zinc collecting agent is added, the process conditions of the zinc scavenging 2 are that 20-50g/t of zinc activator copper sulfate is added, 1-4g/t of zinc collecting agent is added, scavenging foam is returned to the previous operation in sequence, and tailings enter the next sulfur-selecting operation.
4. The method according to claim 1, wherein: in the step (4), the sulfur roughing foam is added with a collector and stirred for first-stage concentration, and the first-stage concentration foam is stirred for second-stage concentration, wherein the second-stage concentration concentrate is sulfur concentrate; adding a sulfur activator and a sulfur collector into the sulfur roughing middlings, performing first-stage scavenging, and returning scavenging foam to the sulfur roughing operation sequentially to obtain sulfur tailings h; 50-120g/t of copper sulfate as an iron sulfide activator is added in the rough concentration of sulfur, 100-200g/t of sulfur collector is added in the rough concentration of sulfur, the technological conditions of sulfur concentration 1 are that 5-10g/t of iron sulfide collector is added in the rough concentration of sulfur, and the secondary concentration is carried out after stirring, wherein the secondary concentrate is sulfur concentrate; the process conditions of the zinc scavenging 1 are that 10-30g/t of copper sulfate as a sulfur activator and 10-20g/t of a sulfur collector are added, scavenging foam is sequentially returned to sulfur roughing operation, and the sulfur tailings are the final tailings.
5. The method according to claim 1, wherein: the pH value is 6-8.
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