[go: up one dir, main page]

WO2024255008A1 - Procédé de raffinage au feu pour plomb d'œuvre complexe - Google Patents

Procédé de raffinage au feu pour plomb d'œuvre complexe Download PDF

Info

Publication number
WO2024255008A1
WO2024255008A1 PCT/CN2023/119268 CN2023119268W WO2024255008A1 WO 2024255008 A1 WO2024255008 A1 WO 2024255008A1 CN 2023119268 W CN2023119268 W CN 2023119268W WO 2024255008 A1 WO2024255008 A1 WO 2024255008A1
Authority
WO
WIPO (PCT)
Prior art keywords
lead
silver
copper
content
antimony
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/CN2023/119268
Other languages
English (en)
Chinese (zh)
Inventor
李一夫
杨斌
徐宝强
田阳
蒋文龙
王凯
张环
马进萍
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Kunming University of Science and Technology
Original Assignee
Kunming University of Science and Technology
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Kunming University of Science and Technology filed Critical Kunming University of Science and Technology
Priority to MX2024014697A priority Critical patent/MX2024014697A/es
Publication of WO2024255008A1 publication Critical patent/WO2024255008A1/fr
Anticipated expiration legal-status Critical
Pending legal-status Critical Current

Links

Classifications

    • 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
    • C22B13/00—Obtaining lead
    • C22B13/06—Refining
    • C22B13/10—Separating metals from lead by crystallising, e.g. by Pattison process
    • 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

Definitions

  • the invention relates to a complex crude lead pyrometallurgical refining method, belonging to the technical field of nonferrous metal metallurgy.
  • Lead is cheap, has high production volume, and has excellent corrosion and radiation resistance. It is widely used in chemical, cable, battery, and radioactive protection industries. In 2021, my country's refined lead production and consumption ranked first in the world. my country's lead ore resources face problems such as more poor ores, fewer rich ores, and high impurity content. Among them, the content of copper, tin, arsenic, antimony, and bismuth is high, which brings severe challenges to the lead refining process.
  • Crude lead refining usually includes pyrometallurgy and electrolytic refining.
  • pyrometallurgy At present, there are many companies in the world that use pyrometallurgy to refine crude lead, accounting for about 70% of the refined output.
  • Foreign lead ore has few impurities, and crude lead obtained by reduction smelting is mainly refined by pyrometallurgy; domestic lead ore has many types of impurities, and crude lead obtained by reduction smelting is mainly refined by electrolytic refining.
  • crude lead is first smelted to remove copper, then sulfur is added to deeply remove copper, alkali is added to remove tin, arsenic and antimony, zinc is added to remove silver, zinc is removed, and bismuth is removed to finally obtain refined lead.
  • the smelting method is used for preliminary copper removal, which can theoretically remove copper to 0.06%, and then sulfur is added to deeply remove copper to 0.001-0.005%; sodium hydroxide and sodium nitrate are generally used to remove arsenic, antimony and tin impurities by oxidation and removal; silver is removed by adding zinc to enrich the silver in the silver-zinc shell; some residual zinc after silver removal can be removed by oxidation, chlorination, alkali and vacuum methods; bismuth is removed by adding calcium and magnesium.
  • each impurity is removed by adding agents to form slag, which requires the addition of a large amount of reagents, a large amount of slag, high energy consumption, a long and time-consuming process, serious environmental pollution, and the introduction of a large number of new impurities.
  • electrolytic refining copper and tin are initially removed from crude lead, anode plates are cast, and cathode lead and anode mud are obtained by electrolysis in electrolyte.
  • the cathode lead is cast into lead ingots.
  • Precious metals are enriched in anode mud, and the lead anode mud must be obtained during the entire lead refining process, and finally recovered from the lead anode mud.
  • the electrolytic refining product is of high quality and is particularly suitable for processing crude lead with high silver and bismuth content. At the same time, it takes a long time to exist, requires large investment, produces a lot of waste liquid, and has a long precious metal recovery cycle.
  • Preliminary fire refining mainly removes copper and tin. After removing the tin copper, it is cast into anode plates for electrolysis to produce electrolytic lead. Preliminary fire refining is required in the lead refining process, which will result in a long refining process, large construction investment, and the generation of a large amount of waste liquid.
  • the patent with publication number CN201210031769.0 discloses a method for direct electrolytic refining of crude lead, wherein crude lead is cast into a crude lead anode which is placed in an anode bag, and electrolysis is performed in an additive and perchloric acid-lead perchlorate electrolyte, and the lead in the anode is electrodeposited on the cathode to obtain electrolytic lead at the cathode and anode mud at the anode.
  • the crude lead is directly electrolytically refined without pre-refining, and the high content of impurity elements such as tin and copper in the crude lead affects the electrolysis efficiency.
  • Tin will enter the cathode lead, which will reduce the quality of the cathode lead, and even the impurity content is high, and the lead ingot is unqualified, and a new process is needed to remove some impurities.
  • the patent with publication number CN201810619887.0 discloses a method for fire refining of complex crude lead, wherein the crude lead melt is oxidized at 800-850°C to obtain lead liquid, the obtained lead liquid is reoxidized at 850-900°C to obtain smoke-like lead oxide, the obtained smoke-like lead oxide is reduced to obtain a reduced product, and the obtained reduced product is repeatedly treated to obtain refined lead. This method requires repeated oxidation and reduction, has high energy consumption, large slag volume, and does not specifically recover precious metals.
  • the patent with publication number CN87104574 discloses a new technology for fire refining of crude lead, wherein the crude lead is subjected to smelting-addition of sulfur to remove copper, alkaline compressed air and oxygen to remove arsenic, antimony and tin, and then crystallization to remove silver and bismuth to obtain refined lead and silver-rich lead, the silver-rich lead is vacuum distilled to obtain crude silver and refined lead or lead alloy, the crude silver is electrolyzed to obtain electrosilver and anode mud, and gold is recovered from the anode mud.
  • This method requires that the impurity silver content in the crude lead be less than 1%, and the bismuth content be 0.02-0.2%.
  • the present invention adopts the method of condensation-crystallization-slag making to refine lead and remove impurities from complex crude lead, so as to solve the problems of multiple impurity types and high content in crude lead, complex process and high smelting cost.
  • the present invention provides a complex crude lead pyrometallurgical refining method.
  • the method has simple process, convenient operation, simple required equipment, low cost, high suitability of raw materials, and safe and controllable process.
  • the present invention is implemented by the following technical solutions.
  • a complex crude lead pyrometallurgical refining method adopts condensation-crystallization-slag making to refine lead, wherein the complex crude lead is condensed, mainly for removing copper, and other impurities such as tin, arsenic, antimony, etc. are also removed in large quantities to obtain low-copper lead and copper scum I; the low-copper lead is continuously crystallized, mainly for removing silver and bismuth, and other impurities such as antimony, arsenic, tin, copper, etc.
  • low-silver lead and high-silver lead are also partially removed to obtain low-silver lead and high-silver lead; the low-silver lead is deeply decoppered by adding sulfur to obtain copper-removed lead and copper scum II; the copper-removed lead is added with alkali to remove arsenic, antimony, and tin to obtain refined lead and arsenic, antimony, and tin slag, and the specific steps include:
  • the complex crude lead is condensed to obtain low-copper lead and copper scum I.
  • copper will condense and precipitate, and part of the copper will form high-melting point compounds with arsenic, antimony and tin, floating on the lead liquid.
  • These high-melting point compounds are copper scum, which are removed by scooping out the scum, and low-copper lead is obtained under the scum.
  • step (2) removing silver and bismuth from the low-copper lead obtained in step (1) by crystallization to obtain low-silver lead and high-silver lead;
  • step (3) adding sulfur to the low-silver lead obtained in step (2) to perform deep copper removal to obtain copper-removed lead and copper slag II;
  • step (3) Add alkali to the copper-free lead obtained in step (3) to obtain refined lead and arsenic, antimony and tin slag.
  • the complex crude lead of step (1) comprises lead, copper, tin, arsenic, antimony, silver, bismuth, zinc, iron, chromium and nickel, wherein the lead content is 78.5-99.5wt%, the copper content is 0.01-5.5wt%, the tin content is 0.01-3.2wt%, the arsenic content is 0.02-5.6wt%, the antimony content is 0.02-5.2wt%, the silver content is 0.02-1.5wt%, the bismuth content is 0.01-0.5wt%, and the nickel, iron, zinc and chromium content are all less than 0.1wt%.
  • the sum of the above metal contents is 100%.
  • the condensation process of step (1) is to first heat up to 480-960°C, then cool down to 320-446°C for condensation, with a cooling rate of 2-8°C/min and a condensation time of 1-5h.
  • the condensed copper scum is separated by centrifugation to obtain low-copper lead, which can reduce the slag production rate and improve the metal recovery rate.
  • the crystallization enrichment equipment in the step (2) of crystallizing and enriching silver has an inclination angle of 4-12°, a rotation speed of 3-11 r/min, a temperature gradient of 304-335°C, a temperature gradient increment greater than 0.1°C, a high silver lead discharge time interval of 8-52 min/time, a discharge time of 20-80 s, and a processing capacity of 1-30 tons/(unit ⁇ day).
  • the sulfur-adding deep decopperizing reagent in step (3) is sulfur, the temperature is 328-360° C., and the stirring speed is 2-20 r/min.
  • the reagents for removing arsenic, antimony and tin by alkaline method are sodium nitrate (NaNO 3 ) and sodium hydroxide (NaOH), and the operating temperature is 380-480° C.
  • the copper scum I obtained in step (1) and the copper scum II obtained in step (3) are recovered and processed.
  • the arsenic, antimony and tin slag obtained in step (4) is recovered and processed.
  • the high-silver lead obtained in step (2) is more than 3 times rich in silver.
  • the high-silver lead obtained in step (2) is sent to a silver refining step.
  • the direct recovery rate of silver in the high-silver lead in the above step (2) is greater than 92%.
  • the crystallization enrichment equipment in the above step (2) is an existing crystallization enrichment equipment, which is the equipment disclosed in the application publication number CN113999992A.
  • the step (1) condensation refers to the process of liquid phase transformation into solid phase in non-ferrous metal metallurgy.
  • the purity of the refined lead is above 99.94wt%, the copper content is less than 0.005wt%, the tin content is less than 0.001wt%, the arsenic content is less than 0.001wt%, the antimony content is less than 0.001wt%, the silver content is less than 0.008wt%, the bismuth content is less than 0.06wt%, the zinc content is less than 0.0005wt%, the iron content is less than 0.002wt%, the chromium content is less than 0.002wt%, and the nickel content is less than 0.002wt%.
  • the lead recovery rate in the above method of the present invention is above 99.96%.
  • the present invention adopts the condensation method to remove a large amount of copper, tin, arsenic and antimony, with a short process and low smelting cost.
  • the low-copper lead of the present invention removes silver and bismuth by crystallization (physical method), and the silver and bismuth are enriched in the high-silver lead without introducing new impurities, and the direct recovery rate of silver is high.
  • the present invention enriches a large amount of arsenic, antimony, tin and copper in high-silver lead through crystallization, and only a small amount of tin, arsenic, antimony and copper remains in low-silver lead, thereby greatly reducing the use of lead refining additives.
  • the "condensation-crystallization-slag-making" fire-refining lead process of the present invention belongs to a physical method, with a short smelting cycle, low energy consumption, low investment and simple equipment.
  • the raw material of the present invention has high adaptability and can be used for various complex crude lead with high metal recovery rate.
  • the cycle of lead refining by the "condensation-crystallization-slag making” method of the present invention is 1 day, and the energy consumption is 250-300 (kW ⁇ h/t).
  • the present invention adopts the method of "condensation-crystallization-slag making" to refine lead, changing the traditional six-step refining into four-step refining.
  • the silver recovery cycle is shortened by 20%-30% compared with the traditional method, the lead refining cycle is shortened by 10%-30%, and the energy consumption is reduced by 10-20%.
  • the present invention has obvious economic benefits and can be fully industrialized.
  • Fig. 1 is a process flow chart of the present invention
  • Figure 2 is a physical picture of the raw materials and some refined lead products of Example 1 of the present invention; (a) is a complex crude lead raw material, and (b) is a part of the refined lead product.
  • the complex crude lead pyrometallurgical refining method adopts condensation-crystallization-slag making to refine lead, and the specific steps include:
  • step (2) Remove silver and bismuth from the low copper lead obtained in step (1) by crystallization.
  • the crystallization enrichment equipment is 3m long, 0.52m wide and 0.31m deep.
  • the equipment slope is adjusted to 8°, the rotation speed is 3r/min, the temperature gradient is 305°C-335°C, and the temperature gradient of the equipment increases from low to high as follows: 305°C, 314°C, 320°C, 325°C, 330°C, 335°C, to obtain low silver lead and high silver lead; put the low copper lead melt into the crystallization enrichment silver equipment, when the melt covers the screw shaft, slow down the liquid inlet flow rate, precipitate crystals by natural cooling, and transport the crystals by spiral to high temperature melting and purification to obtain low silver lead, and the molten liquid is refluxed to the low temperature section for further crystallization.
  • the lead content in the low temperature section decreases, and the silver, bismuth, arsenic, antimony and tin content increases to obtain high silver lead.
  • the high silver lead is discharged at a time interval of 30min and the discharge time is 20s.
  • the quality and composition of low silver lead and high silver lead are shown in Table 1. The operation lasts for 9 hours;
  • step (3) The low-silver lead obtained in step (2) was subjected to a deep decoppering operation by adding sulfur (sulfur, the amount of sulfur added was 3.01 kg), the operating temperature was 350°C, the stirring rate was 8 r/min, and copper-free lead (mass and composition table are shown in Table 1) and copper slag II were obtained. The operation lasted for 2 hours.
  • step (3) The copper-free lead obtained in step (3) was subjected to an alkali-adding operation to remove arsenic, antimony and tin.
  • an alkali-adding operation to remove arsenic, antimony and tin.
  • NaNO 3 sodium nitrate
  • NaOH sodium hydroxide
  • the low-silver lead obtained by crystallization contains 0.0024% silver, which is lower than the silver content in Pb99.985 grade.
  • the silver direct recovery rate is 96.59%.
  • the high-silver lead contains 0.39% silver, and the silver is enriched by 3.28 times.
  • the low-silver lead contains 0.001% copper.
  • the arsenic content is 0.0005%, and the antimony content is 0.0008%. All impurities reach Pb99.970 grade.
  • the complex crude lead pyrometallurgical refining method adopts condensation-crystallization-slag making to refine lead, and the specific steps include:
  • the crystallization enrichment equipment is 3m long, 0.52m wide and 0.31m deep.
  • the equipment slope is adjusted to 12°, the rotation speed is 3r/min, the temperature gradient is 305°C-335°C, and the temperature gradient of the equipment increases from low to high as follows: 305°C, 315°C, 320°C, 325°C, 330°C, 335°C, to obtain low silver lead and high silver lead; put the low copper lead melt into the crystallization enrichment silver equipment, when the melt covers the screw shaft, slow down the liquid inlet flow rate, precipitate crystals by natural cooling, and transport the crystals by spiral to high temperature melting and purification to obtain low silver lead, and the molten liquid is refluxed to the low temperature section for further crystallization.
  • the lead content in the low temperature section decreases, and the silver, bismuth, arsenic, antimony and tin content increases to obtain high silver lead.
  • the high silver lead discharge time interval is 50min, and the discharge time is 60s.
  • the quality and composition of low silver lead and high silver lead are shown in Table 3. The operation lasts 11 hours;
  • step (3) The low-silver lead obtained in step (2) was subjected to a deep decoppering operation by adding sulfur (sulfur, the amount of sulfur added was 2.61 kg), the operating temperature was 360°C, the stirring rate was 15 r/min, and copper-free lead (mass and composition table are shown in Table 3) and copper slag II were obtained. The operation lasted for 2.5 hours.
  • step (3) The copper-free lead obtained in step (3) was subjected to an alkali-adding operation to remove arsenic, antimony and tin.
  • an alkali-adding operation to remove arsenic, antimony and tin.
  • NaNO 3 sodium nitrate
  • NaOH sodium hydroxide
  • the low-silver lead obtained by crystallization contains 0.0051% silver, which is lower than the silver content in Pb99.940 grade.
  • the silver direct recovery rate is 92.77%.
  • the high-silver lead contains 1.59% silver, and the silver is enriched by 4.72 times.
  • the low-silver lead contains 0.001% copper.
  • the arsenic content is 0.0005%
  • the antimony content is 0.0005%. All impurities reach Pb99.970 grade.
  • the complex crude lead pyrometallurgical refining method adopts condensation-crystallization-slag making to refine lead, and the specific steps include:
  • step (2) Remove silver and bismuth from the low copper lead obtained in step (1) by crystallization.
  • the crystallization enrichment equipment is 4m long, 0.61m wide and 0.42m deep.
  • the equipment slope is adjusted to 10°, the rotation speed is 10r/min, the temperature gradient is 305°C-335°C, and the temperature gradient of the equipment increases from low to high as follows: 305°C, 313°C, 320°C, 325°C, 331°C, 335°C, to obtain low silver lead and high silver lead; put the low copper lead melt into the crystallization enrichment silver equipment, when the melt covers the screw shaft, slow down the liquid inlet flow rate, precipitate crystals by natural cooling, and transport the crystals by spiral to high temperature melting and purification to obtain low silver lead, and the molten liquid is refluxed to the low temperature section for further crystallization.
  • the lead content in the low temperature section decreases, and the silver, bismuth, arsenic, antimony and tin content increases to obtain high silver lead.
  • the high silver lead discharge time interval is 10min, and the discharge time is 20s.
  • the quality and composition of low silver lead and high silver lead are shown in Table 5. The operation lasts for 12 hours;
  • step (3) The low-silver lead obtained in step (2) was subjected to a deep decoppering operation by adding sulfur (sulfur, the amount of sulfur added was 115 kg), the operating temperature was 360°C, the stirring rate was 10 r/min, and copper-free lead (the mass and composition table are shown in Table 5) and copper slag II were obtained. The operation lasted for 2 hours.
  • step (3) The copper-free lead obtained in step (3) was subjected to an alkali-adding operation to remove arsenic, antimony and tin.
  • an alkali-adding operation to remove arsenic, antimony and tin.
  • NaNO 3 sodium nitrate
  • NaOH sodium hydroxide
  • the low-silver lead obtained by crystallization contains 0.0056% silver, which is lower than the silver content in Pb99.940 grade.
  • the high-silver lead contains 1.166% silver, and the silver is enriched by 5.61 times.
  • the low-silver lead contains 0.004% copper after deep decoppering with sulfur. After copper-free lead is refined with alkali, the arsenic content is 0.001%, and the antimony content is 0.0008%. All impurities reach Pb99.940 grade.
  • the complex crude lead pyrometallurgical refining method adopts condensation-crystallization-slag making to refine lead, and the specific steps include:
  • the low copper lead obtained in step (1) is crystallized to remove silver and bismuth.
  • the crystallization enrichment equipment is 4m long, 0.61m wide and 0.42m deep.
  • the equipment slope is adjusted to 10°, the rotation speed is 6r/min, the temperature gradient is 305°C-335°C, and the temperature gradient of the equipment increases from low to high as follows: 305°C, 312°C, 318°C, 325°C, 329°C, 335°C, to obtain low silver lead and high silver lead; the low copper lead melt is placed in the crystallization enrichment silver equipment.
  • the liquid inlet flow rate is slowed down, and the crystals are precipitated by natural cooling.
  • the crystals are transported to high temperature melting and purification by the spiral to obtain low silver lead.
  • the molten liquid is refluxed to the low temperature section for further crystallization.
  • the lead content in the low temperature section is reduced, and the silver, bismuth, arsenic, antimony and tin content is increased to obtain high silver lead.
  • the high silver lead is discharged at a time interval of 45min and the discharge time is 50s.
  • the quality and composition of low silver lead and high silver lead are shown in Table 7. The operation lasts for 16 hours.
  • step (3) The low-silver lead obtained in step (2) was subjected to a deep decoppering operation by adding sulfur (sulfur, the amount of sulfur added was 6.86 kg), the operating temperature was 338°C, the stirring rate was 6 r/min, and copper-free lead (the mass and composition table are shown in Table 7) and copper slag II were obtained. The operation lasted for 2 hours.
  • step (3) The copper-free lead obtained in step (3) was subjected to an alkali-adding operation to remove arsenic, antimony and tin.
  • an alkali-adding operation to remove arsenic, antimony and tin.
  • NaNO 3 sodium nitrate
  • NaOH sodium hydroxide
  • the low-silver lead obtained by crystallization contains 0.0019% silver, which is lower than the silver content in Pb99.985 grade.
  • the high-silver lead contains 0.39% silver, and the silver is enriched by 3.25 times.
  • the low-silver lead contains 0.001% copper.
  • the arsenic content is 0.001%, and the antimony content is 0.001%. All impurities reach Pb99.970 grade.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

Procédé de raffinage au feu pour plomb d'œuvre complexe appartenant au domaine technique de la métallurgie non ferreuse. Le procédé consiste à : condenser du plomb d'œuvre complexe de façon à obtenir du plomb à faible teneur en cuivre et des scories de cuivre I ; cristalliser le plomb à faible teneur en cuivre obtenu pour éliminer l'argent et le bismuth de façon à obtenir du plomb à faible teneur en argent et du plomb à haute teneur en argent ; ajouter du soufre au plomb à faible teneur en argent obtenu pour éliminer en profondeur le cuivre de façon à obtenir du plomb sans cuivre et des scories de cuivre II ; et éliminer l'arsenic, l'antimoine et l'étain du plomb sans cuivre obtenu par l'intermédiaire d'un procédé alcalin de façon à obtenir du plomb raffiné et des scories d'arsenic-antimoine-étain. En utilisant le procédé de « condensation-cristallisation-scorification » pour le raffinage de plomb, la présente invention transforme les six étapes de raffinage classiques en quatre étapes de raffinage, la durée de raffinage du plomb étant raccourcie de 10 % à 30 %, la durée de récupération de l'argent étant de 20 % à 30 % plus courte que celles de procédés classiques, la consommation d'énergie étant réduite de 10 à 20 % et la quantité de réactifs étant réduite de 30 % à 60 %, ce qui permet d'obtenir des avantages économiques significatifs et une application industrielle.
PCT/CN2023/119268 2023-06-12 2023-09-16 Procédé de raffinage au feu pour plomb d'œuvre complexe Pending WO2024255008A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
MX2024014697A MX2024014697A (es) 2023-06-12 2024-11-27 Metodo de refinado por tratamiento termico de plomo crudo complejo

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN202310687414.5A CN116411175B (zh) 2023-06-12 2023-06-12 一种复杂粗铅火法精炼方法
CN202310687414.5 2023-06-12

Publications (1)

Publication Number Publication Date
WO2024255008A1 true WO2024255008A1 (fr) 2024-12-19

Family

ID=87056339

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2023/119268 Pending WO2024255008A1 (fr) 2023-06-12 2023-09-16 Procédé de raffinage au feu pour plomb d'œuvre complexe

Country Status (3)

Country Link
CN (1) CN116411175B (fr)
MX (1) MX2024014697A (fr)
WO (1) WO2024255008A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116411175B (zh) * 2023-06-12 2023-08-25 昆明理工大学 一种复杂粗铅火法精炼方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA1225242A (fr) * 1984-10-18 1987-08-11 John G. Peacey Amollissement a haute temperature des lingots de plomb
CN87104574A (zh) * 1987-06-27 1988-03-30 昆明工学院 粗铅火法精炼新技术
CN102011015A (zh) * 2010-12-21 2011-04-13 株洲冶炼集团股份有限公司 一种粗铅精炼脱除砷、锑、铜的方法
CN103540762A (zh) * 2012-07-11 2014-01-29 陕西锌业有限公司 一种工频无心感应电炉熔铅除铜精炼工艺
CN108893621A (zh) * 2018-06-15 2018-11-27 昆明理工大学 一种火法精炼粗铅的方法
CN116411175A (zh) * 2023-06-12 2023-07-11 昆明理工大学 一种复杂粗铅火法精炼方法

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB123272A (en) * 1918-08-06 1919-02-20 George Powell Hulst Process of Treating Lead Bullion.
GB1360692A (en) * 1972-08-04 1974-07-17 American Smelting Refining Process for de-copperizing lead
US8211207B2 (en) * 2006-12-05 2012-07-03 Stannum Group LLC Process for refining lead bullion
CN101358286B (zh) * 2008-09-25 2010-06-16 昆明理工大学 用转炉处理铜浮渣的方法
CN101525694B (zh) * 2009-04-17 2011-01-19 深圳市中金岭南有色金属股份有限公司韶关冶炼厂 含铅锑铜铋银物料的分离工艺
CN103131869A (zh) * 2013-03-13 2013-06-05 山东恒邦冶炼股份有限公司 高铅高银含砷复杂金精矿的提取方法
CN103667737A (zh) * 2013-12-31 2014-03-26 湖南省桂阳银星有色冶炼有限公司 一种粗铅火法初步精炼方法
KR102355322B1 (ko) * 2017-04-10 2022-01-25 메탈로 벨지움 크루드 솔더의 제조를 위한 개선된 방법
CA3126515A1 (fr) * 2019-01-30 2020-08-06 Metallo Belgium Procede ameliore de production de plomb de haute purete
CN113737007B (zh) * 2021-07-28 2023-03-17 昆明理工大学 一种高锑粗锡分离提纯的方法
CN113684386A (zh) * 2021-08-17 2021-11-23 尤全仁 一种粗杂铅精炼再生铅锡基多元素合金的方法
CN115369262B (zh) * 2022-09-20 2023-08-01 云南锡业股份有限公司锡业分公司 一种复杂粗锡绿色高效的精炼方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA1225242A (fr) * 1984-10-18 1987-08-11 John G. Peacey Amollissement a haute temperature des lingots de plomb
CN87104574A (zh) * 1987-06-27 1988-03-30 昆明工学院 粗铅火法精炼新技术
CN102011015A (zh) * 2010-12-21 2011-04-13 株洲冶炼集团股份有限公司 一种粗铅精炼脱除砷、锑、铜的方法
CN103540762A (zh) * 2012-07-11 2014-01-29 陕西锌业有限公司 一种工频无心感应电炉熔铅除铜精炼工艺
CN108893621A (zh) * 2018-06-15 2018-11-27 昆明理工大学 一种火法精炼粗铅的方法
CN116411175A (zh) * 2023-06-12 2023-07-11 昆明理工大学 一种复杂粗铅火法精炼方法

Also Published As

Publication number Publication date
MX2024014697A (es) 2025-02-10
CN116411175A (zh) 2023-07-11
CN116411175B (zh) 2023-08-25

Similar Documents

Publication Publication Date Title
CN105695744B (zh) 一种多金属全路径全价分离方法
CN101078052B (zh) 从钢铁厂固废物中综合回收铁和有色金属的方法
CN100569968C (zh) 一种高纯铜及低氧光亮铜杆的生产方法
CN115369262B (zh) 一种复杂粗锡绿色高效的精炼方法
CN107557589B (zh) 一种从湿法炼锌铜镉渣中回收有价金属的方法
CN102643996A (zh) 一种铜浮渣侧吹熔炼生产粗铅的方法
CN102011015A (zh) 一种粗铅精炼脱除砷、锑、铜的方法
CN102828042B (zh) 一种含银粗锡合金中提取银的方法
CN102312097B (zh) 一种从铜阳极泥分银渣制取巴氏合金的方法
CN101260481B (zh) 高纯铅的生产方法
CN116426766B (zh) 一种复杂粗铅提银的方法
CN115927859A (zh) 一种硫酸铜循环浸出中冰镍回收有价金属的方法
WO2024255008A1 (fr) Procédé de raffinage au feu pour plomb d'œuvre complexe
CN87104574A (zh) 粗铅火法精炼新技术
CN103668323B (zh) 一种电解-分段电积法处理含铜镍物料的方法
CN115627367B (zh) 一种铅和锑协同冶炼的方法
CN116445740A (zh) 一种铅锑合金的分离方法
CN111549233B (zh) 从铜阳极泥熔炼渣中回收铅铋的方法
CN1295135A (zh) 铅锑合金冶炼的除砷方法
CN104928491B (zh) 一种向含银锡合金中加木屑除银的方法
WO2025000493A1 (fr) Procédé de préparation d'une substance élémentaire de fer à pureté élevée à partir de laitier de fusion de minerai de latérite-nickel
CN114058878A (zh) 一种在含锡物料冶炼过程中有效降低铜渣中锡含量的方法
CN109778230B (zh) 一种高铅冰铜电解分离铅和铜的方法
CN114182105A (zh) 一种从复杂多金属铅搅铜渣中回收有价金属的方法
CN114855025B (zh) 一种利用回收铝制备电机转子铝合金的方法和应用

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: MX/A/2024/014697

Country of ref document: MX

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 23941233

Country of ref document: EP

Kind code of ref document: A1

WWP Wipo information: published in national office

Ref document number: MX/A/2024/014697

Country of ref document: MX