In Situ Resource Recovery from Waste Repositories: Exploring the Potential for Mobilization and Capture of Metals from Anthropogenic Ores
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Principles of Extractive Metallurgy Lectures Note
PRINCIPLES OF EXTRACTIVE METALLURGY B.TECH, 3RD SEMESTER LECTURES NOTE BY SAGAR NAYAK DR. KALI CHARAN SABAT DEPARTMENT OF METALLURGICAL AND MATERIALS ENGINEERING PARALA MAHARAJA ENGINEERING COLLEGE, BERHAMPUR DISCLAIMER This document does not claim any originality and cannot be used as a substitute for prescribed textbooks. The information presented here is merely a collection by the author for their respective teaching assignments as an additional tool for the teaching-learning process. Various sources as mentioned at the reference of the document as well as freely available material from internet were consulted for preparing this document. The ownership of the information lies with the respective author or institutions. Further, this document is not intended to be used for commercial purpose and the faculty is not accountable for any issues, legal or otherwise, arising out of use of this document. The committee faculty members make no representations or warranties with respect to the accuracy or completeness of the contents of this document and specifically disclaim any implied warranties of merchantability or fitness for a particular purpose. BPUT SYLLABUS PRINCIPLES OF EXTRACTIVE METALLURGY (3-1-0) MODULE I (14 HOURS) Unit processes in Pyro metallurgy: Calcination and roasting, sintering, smelting, converting, reduction, smelting-reduction, Metallothermic and hydrogen reduction; distillation and other physical and chemical refining methods: Fire refining, Zone refining, Liquation and Cupellation. Small problems related to pyro metallurgy. MODULE II (14 HOURS) Unit processes in Hydrometallurgy: Leaching practice: In situ leaching, Dump and heap leaching, Percolation leaching, Agitation leaching, Purification of leach liquor, Kinetics of Leaching; Bio- leaching: Recovery of metals from Leach liquor by Solvent Extraction, Ion exchange , Precipitation and Cementation process. -
Understanding Fluid–Rock Interactions and Lixiviant/Oxidant Behaviour for the In-Situ Recovery of Metals from Deep Ore Bodies
School of Earth and Planetary Science Department of Applied Geology Understanding Fluid–Rock Interactions and Lixiviant/Oxidant Behaviour for the In-situ Recovery of Metals from Deep Ore Bodies Tania Marcela Hidalgo Rosero This thesis is presented for the degree of Doctor of Philosophy of Curtin University February 2020 1 Declaration __________________________________________________________________________ Declaration To the best of my knowledge and belief, I declare that this work of thesis contains no material published by any other person, except where due acknowledgements have been made. This thesis contains no material which has been accepted for the award of any other degree or diploma in any university. Tania Marcela Hidalgo Rosero Date: 28/01/2020 2 Abstract __________________________________________________________________________ Abstract In-situ recovery (ISR) processing has been recognised as a possible alternative to open- pit mining, especially for low-grade resources. In ISR, the fluid–rock interaction between the target ore and the lixiviant results in valuable- (and gangue-) metal dissolution. This interaction is achieved by the injection and recovery of fluid by means of strategically positioned wells. Although the application of ISR has become more common (ISR remains the preferential processing technique for uranium and has been applied in pilot programs for treating oxide zones in copper deposits), its application to hard-rock refractory and low-grade copper-sulfide deposits is still under development. This research is focused on the possible application of ISR to primary copper sulfides usually found as deep ores. Lixiviant/oxidant selection is an important aspect to consider during planning and operation in the ISR of copper-sulfide ores. -
Treatment and Microscopy of Gold
TREATMENT AND MICROSCOPY OF GOLD AND BASE METAL ORES. (Script with Sketches & Tables) Short Course by R. W. Lehne April 2006 www.isogyre.com Geneva University, Department of Mineralogy CONTENTS (Script) page 1. Gold ores and their metallurgical treatment 2 1.1 Gravity processes 2 1.2 Amalgamation 2 1.3 Flotation and subsequent processes 2 1.4 Leaching processes 3 1.5 Gold extraction processes 4 1.6 Cyanide leaching vs. thio-compound leaching 5 2. Microscopy of gold ores and treatment products 5 2.1 Tasks and problems of microscopical investigations 5 2.2 Microscopy of selected gold ores and products 6 (practical exercises) 3. Base metal ores and their beneficiation 7 3.1 Flotation 7 3.2 Development of the flotation process 7 3.3 Principles and mechanisms of flotation 7 3.4 Column flotation 9 3.5 Hydrometallurgy 10 4. Microscopy of base metal ores and milling products 10 4.1 Specific tasks of microscopical investigations 11 4.2 Microscopy of selected base metal ores and milling products 13 (practical exercises) 5. Selected bibliography 14 (Sketches & Tables) Different ways of gold concentration 15 Gravity concentration of gold (Agricola) 16 Gravity concentration of gold (“Long Tom”) 17 Shaking table 18 Humphreys spiral concentrator 19 Amalgamating mills (Mexican “arrastra”, Chilean “trapiche”) 20 Pressure oxidation flowsheet 21 Chemical reactions of gold leaching and cementation 22 Cyanide solubilities of selected minerals 23 Heap leaching flowsheet 24 Carbon in pulp process 25 Complexing of gold by thio-compounds 26 Relation gold content / amount of particles in polished section 27 www.isogyre.com Economically important copper minerals 28 Common zinc minerals 29 Selection of flotation reagents 30 Design and function of a flotation cell 31 Column cell flotation 32 Flowsheet of a simple flotation process 33 Flowsheet of a selective Pb-Zn flotation 34 Locking textures 35 2 1. -
Xstrata Technology Update Edition 13 – April 2012 Building Plants That Work
xstrata technology update Edition 13 – April 2012 Building plants that work You have to get a lot of things it takes another operator to get them right to build a plant that works. right. Someone who has lived through the problems, had to do the maintenance, operated during a midnight power Of course the big picture must be right – doing the right project, in the right place, failure, cleaned up the spill. Someone at the right time. who has “closed the loop” on previous designs; lived with previous decisions After that, the devil is in the detail. You and improved them, over and over. need a sound design, good execution, good commissioning, and ongoing This is why Xstrata Technology provides support after commissioning. You need a technology “package”. Just as a car to operate and maintain your plant in is more than an engine, technology is the long run, long after the construction more than a single piece of equipment. company has left. That’s when all the Technology is a system. All the elements “little” details become important – how of the system have to work with each easy is it to operate, how good is the other and with the people in the plant. maintenance access, what happens in We want our cars designed by people a power failure, where are the spillage who love cars and driving. So should points and how do we clean them our plants be designed by people with up? Are the instruments reliable and experience and passion to make each is the process control strategy robust one work better than the last. -
Identification and Description of Mineral Processing Sectors And
V. SUMMARY OF FINDINGS As shown in Exhibit 5-1, EPA determined that 48 commodity sectors generated a total of 527 waste streams that could be classified as either extraction/beneficiation or mineral processing wastes. After careful review, EPA determined that 41 com modity sectors generated a total of 354 waste streams that could be designated as mineral processing wastes. Exhibit 5-2 presents the 354 mineral processing wastes by commodity sector. Of these 354 waste streams, EPA has sufficient information (based on either analytical test data or engineering judgment) to determine that 148 waste streams are potentially RCRA hazardous wastes because they may exhibit one or more of the RCRA hazardous characteristics: toxicity, ignitability, corro sivity, or reactivity. Exhibit 5-3 presents the 148 RCRA hazardous mineral processing wastes that will be subject to the Land Disposal Restrictions. Exhibit 5-4 identifies the mineral processing commodity sectors that generate RCRA hazardous mineral processing wastes that are likely to be subject to the Land D isposal Restrictions. Exhibit 5-4 also summarizes the total number of hazardous waste streams by sector and the estimated total volume of hazardous wastes generated annually. At this time, however, EPA has insufficient information to determine whether the following nine sectors also generate wastes that could be classified as mineral processing wastes: Bromine, Gemstones, Iodine, Lithium, Lithium Carbonate, Soda Ash, Sodium Sulfate, and Strontium. -
Gold Extraction from Paleochannel Ores Using an Aerated Alkaline Glycine Lixiviant for Consideration in Heap and In-Situ Leaching Applications E.A
Gold extraction from paleochannel ores using an aerated alkaline glycine lixiviant for consideration in heap and in-situ leaching applications E.A. Orabya,c, J.J. Eksteena*, A. Karrechb, M. Attarb aFaculty of Science and Engineering, Western Australian School of Mines: Minerals, Energy and Chemical Engineering, Curtin University, GPO Box U1987, Perth, WA 6845, Australia bDepartment of Civil, Environmental and Mining Engineering, The University of Western Australia, Australia c Mining and Metallurgical Engineering, Faculty of Engineering, Assiut University, Egypt *Corresponding Author: [email protected] ABSTRACT The decreasing grades of some gold deposits combined with the increasing depths, difficult surface topography, socioeconomic and geopolitical pressures often make the processing of such deposits infeasible by conventional mining, comminution and leaching technologies. To overcome these problems, the application of in-place, in-situ, and heap leaching often represent an optimal solution that minimises the capital and operating costs associated with mining and processing operations. Non- toxic, low cost lixiviants that are stable over an extended range of pH and Eh are required to provide any practical solution to ISL. Since ISL has the inherent benefit of increased natural rock temperature and pressure, glycine-based systems can be considered to extract valuable metals. Based on earlier studies on glycine leaching of pure gold foil, this research shows that Western Australian paleochannel ores are amenable to glycine-based ISL, at elevated alkalinity. The effects of pH, temperature, free glycine, ferric ions, sodium chloride and solids percentages on the kinetics of gold extraction were assessed. More than 85% of the gold can be extracted from ore with solutions containing 15 g/L glycine at pH 12.5 in 336 hours. -
Copper Recovery Using Leach/Solvent Extraction/Electrowinning Technology
Copper recovery using leach/solvent extraction/electrowinning technology: Forty years of innovation, 2.2 million tonnes of copper annually by G.A. Kordosky* small scale in analytical chemistry3 and on a large scale for the recovery of uranium from Synopsis sulphuric acid leach solutions4. Generally Mills had already developed and commercialized The concept of selectively extracting copper from a low-grade dump Alamine® 336 as an SX reagent for the leach solution followed by stripping the copper into an acid recovery of uranium from sulphuric acid leach solution from which electrowon copper cathodes could be produced liquors5 and believed that a similar technology occurred to the Minerals Group of General Mills in the early 1960s. for copper recovery would be welcome. This simple, elegant idea has resulted in a technology by which However, an extensive market survey showed about 2.2 million tonnes of high quality copper cathode was produced in year 2000. The growth of this technology is traced over that the industry reception for copper recovery time with a discussion of the key plants, the key people and the by L/SX/EW technology was almost hostile. important advances in leaching, plant design, reagents and The R&D director of a large copper producer electrowinning that have contributed to the growth of this predicted at an AIME annual meeting that technology. Some thoughts on potential further advances in the there would never be a pound of copper technology are also given. recovered using solvent extraction and his comment prompted -
Pretreatment of Copper Ore Prior to Heap Leaching Includes Crushing and Agglomeration Processes Which Were Studied in This Thesis Research
PRETREATMENT OF COPPER ORE PRIOR TO HEAP LEACHING by Phanindra Kodali A thesis submitted to the faculty of The University of Utah in partial fulfillment of the requirements for the degree of Master of Science Department of Metallurgical Engineering The University of Utah August 2010 Copyright Phanindra Kodali 2010 All Rights Reserved The University of Utah Graduate School STATEMENT OF THESIS APPROVAL The thesis of Phanindra Kodali has been approved by the following supervisory committee members: Jan D. Miller , Chair 11113/2009 Chen-Luh Lin , Member 11113/2009 Xuming Wang , Member 11113/2009 Michael S. Moats . Member 11113/2009 and by Jan D. Miller , Chair of the Department of Metallurgical Engineering and by Charles A. Wight, Dean of The Graduate School. ABSTRACT Pretreatment of copper ore prior to heap leaching includes crushing and agglomeration processes which were studied in this thesis research. Crushing is a high energy consuming process. In mining operations generally jaw and gyratory crushers are used for primary crushing and cone crushers are used for secondary crushing. During the past couple of decades High Pressure Grinding Roll (HPGR) crushers are being considered by mining companies due to lower energy consumption. In the present research copper ores (copper oxide and copper sulfide ores) were crushed by a jaw crusher and by HPGR and the products evaluated for particle damage, as well as by column leaching to determine the rate and extent of copper recovery. X-ray computed tomography analysis and laboratory column leaching experiments on copper oxide samples revealed that products from HPGR crushing have more particle damage and higher copper recoveries when compared with products from jaw crusher crushing. -
In-Situ Chromium and Vanadium Recovery of Landfilled Ferrochromium
Chemical Engineering Journal 303 (2016) 359–368 Contents lists available at ScienceDirect Chemical Engineering Journal journal homepage: www.elsevier.com/locate/cej In-situ chromium and vanadium recovery of landfilled ferrochromium and stainless steel slags ⇑ Jeroen Spooren a, , Eunyoung Kim a,b, Liesbeth Horckmans a, Kris Broos a, Peter Nielsen a, Mieke Quaghebeur a a VITO – Flemish Institute for Technological Research, Boeretang 200, B-2400 Mol, Belgium b Department of Bioengineering, University of Antwerp, Groenenborgerlaan 171, B-2020 Antwerp, Belgium highlights NaOCl assisted alkaline heap leaching of Cr and V from slags was investigated. The matrix material of stainless steel slag and ferrochromium slag remains intact. 11–19% Cr and 7.0–7.5% V were leached selectively after 64 days. A model shows that Cr will leach for 4–5 years at chosen heap leaching conditions. Cr and V extraction potentially improves the slags’ environmental quality. article info abstract Article history: A novel heap leaching method was investigated for selective removal of chromium (Cr) and vanadium (V) Received 26 March 2016 from ferrochromium (FeCr) and stainless steel (SS) slags. In particular, alkaline oxidative heap leaching Received in revised form 25 May 2016 was simulated on lab-scale by batch and column leaching tests. The results show a selective leaching Accepted 26 May 2016 of Cr (11–19%) and V (7.0–7.5%) after 64 days of column leaching, with a very low dissolution (<2.2% Available online 27 May 2016 (FeCr slag) and <0.15% (SS slag)) of matrix elements (e.g. Al, Fe, Si, Mg, Ca), when NaOCl is applied as oxi- dation agent and NaOH as alkaline agent. -
The Metallurgy of Antimony
Chemie der Erde 72 (2012) S4, 3–8 Contents lists available at SciVerse ScienceDirect Chemie der Erde journal homepage: www.elsevier.de/chemer The metallurgy of antimony Corby G. Anderson ∗ Kroll Institute for Extractive Metallurgy, George S. Ansell Department of Metallurgical and Materials Engineering, Colorado School of Mines, Golden, CO 80401, United States article info abstract Article history: Globally, the primary production of antimony is now isolated to a few countries and is dominated by Received 4 October 2011 China. As such it is currently deemed a critical and strategic material for modern society. The metallurgical Accepted 10 April 2012 principles utilized in antimony production are wide ranging. This paper will outline the mineral pro- cessing, pyrometallurgical, hydrometallurgical and electrometallurgical concepts used in the industrial Keywords: primary production of antimony. As well an overview of the occurrence, reserves, end uses, production, Antimony and quality will be provided. Stibnite © 2012 Elsevier GmbH. All rights reserved. Tetrahedrite Pyrometallurgy Hydrometallurgy Electrometallurgy Mineral processing Extractive metallurgy Production 1. Background bullets and armory. The start of mass production of automobiles gave a further boost to antimony, as it is a major constituent of Antimony is a silvery, white, brittle, crystalline solid that lead-acid batteries. The major use for antimony is now as a trioxide exhibits poor conductivity of electricity and heat. It has an atomic for flame-retardants. number of 51, an atomic weight of 122 and a density of 6.697 kg/m3 ◦ ◦ at 26 C. Antimony metal, also known as ‘regulus’, melts at 630 C 2. Occurrence and mineralogy and boils at 1380 ◦C. -
Study of the Calcination Process of Two Limonitic Iron Ores Between 250 °C and 950 °C
Lisbeth Longa-Avello - Cristina Pereyra-Zerpa - Julio Andrés Casal-Ramos - Pedro Delvasto Study of the calcination process of two limonitic iron ores between 250 °C and 950 °C Estudio del proceso de calcinación en dos minerales de hierro limoníticos entre 250 °C y 950 °C Estudo do processo de calcinação em dois minerais de ferro limoníticos entre 250 °C e 950 °C Lisbeth Longa-Avello* Cristina Pereyra-Zerpa** Fecha de recepción: 20 de septiembre de 2016 Julio Andrés Casal-Ramos*** Fecha de aprobación: 20 de marzo de 2017 Pedro Delvasto**** Abstract The dehydration process of two limonitic ores from Venezuela was studied between 250 °C and 950 °C by means of thermogravimetry, infrared spectroscopy, and x-ray diffraction. These techniques indicated for both minerals that the goethite-to-hematite transformation occurred in the range of 250-350 °C. In addition, the x-ray diffraction showed a structural re-arrangement within the orebody above 350 °C, temperature above which only the hematite structure is recognizable. Finally, infrared spectroscopy revealed that such transformation implies the loss of structural OH- functional groups, characteristic of the limonite. Keywords: Iron Ore; Limonite; Thermal Modification of Minerals. Resumen Se estudió el proceso de deshidratación de dos minerales limoníticos de Venezuela entre 250 °C y 950 °C, usando termogravimetría, espectroscopia infrarroja y difracción de rayos x. Para ambos materiales, estas técnicas indicaron que la transformación de goethita a hematita ocurrió en el rango de 250 °C a 350 °C. Adicionalmente, la difracción de rayos X mostró un rearreglo estructural dentro de la mena a una temperatura por encima de 350 °C; a temperaturas mayores, solo se reconoce la estructura de la hematita. -
Extractive Metallurgy of Copper This Page Intentionally Left Blank Extractive Metallurgy of Copper
Extractive Metallurgy of Copper This page intentionally left blank Extractive Metallurgy of Copper Mark E. Schlesinger Matthew J. King Kathryn C. Sole William G. Davenport AMSTERDAM l BOSTON l HEIDELBERG l LONDON NEW YORK l OXFORD l PARIS l SAN DIEGO SAN FRANCISCO l SINGAPORE l SYDNEY l TOKYO Elsevier The Boulevard, Langford Lane, Kidlington, Oxford OX5 1GB, UK Radarweg 29, PO Box 211, 1000 AE Amsterdam, The Netherlands First edition 1976 Second edition 1980 Third edition 1994 Fourth edition 2002 Fifth Edition 2011 Copyright Ó 2011 Elsevier Ltd. All rights reserved. No part of this publication may be reproduced, stored in a retrieval system or transmitted in any form or by any means electronic, mechanical, photocopying, recording or otherwise without the prior written permission of the publisher Permissions may be sought directly from Elsevier’s Science & Technology Rights Department in Oxford, UK: phone (+44) (0) 1865 843830; fax (+44) (0) 1865 853333; email: permissions@ elsevier.com. Alternatively you can submit your request online by visiting the Elsevier web site at http://elsevier.com/locate/permissions, and selecting Obtaining permission to use Elsevier material Notice No responsibility is assumed by the publisher for any injury and/or damage to persons or property as a matter of products liability, negligence or otherwise, or from any use or operation of any methods, products, instructions or ideas contained in the material herein British Library Cataloguing in Publication Data A catalogue record for this book is available from the British Library Library of Congress Cataloging-in-Publication Data A catalog record for this book is available from the Library of Congress ISBN: 978-0-08-096789-9 For information on all Elsevier publications visit our web site at elsevierdirect.com Printed and bound in Great Britain 11 12 13 14 10 9 8 7 6 5 Photo credits: Secondary cover photograph shows anode casting furnace at Palabora Mining Company, South Africa.