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Soil Regions of the European Union and Adjacent Countries 1:5,000,000 (WMS)

The map of the "Soil Regions of the European Union and Adjacent Countries 1:5,000,000 (Version 2.0)" is published by the Federal Institute of Geosciences and Natural Resources (BGR), in partnership with the Joint Research Center (JRC, Ispra). The soil regions map is intended to support the current national mapping activities towards a European 1:250,000 datbase by stratifying similar regional soil associations into a hierarchical concept. Only by stratification, the complexity of soils can be systematically structured so that the complex 1:250,000 legend can be handled in cross-national and contintental-level applications. Soil regions are natural, cross-regional soil geographical units which perform the highest spatial and content-based aggregation of European soils. They represent the frame conditions for soil development at the landscape level. The soil regions are presented at scale 1:5,000,000. Thus, its borders are highly generalized. Because of its low resolution, the map units absorb atypical soils and associations of soils, which are only described in higher resolution soil maps. The delineation of the soil regions is expected to be refined (and probably improved by its content) during the actual 1:250,000 mapping process. Thus, updating can be expected in the future. Currently, the soil regions map is the only graphical soil representation in Europe which has been developed using fully comparable and harmonized basic data at the continental level (climate, hydrography, relief, geology, vegetation): the interpretation of this input data, and the utilization of expert knowledge (including the interpretation of regional soil maps) has been done using one common methodology, developed and applied consistently throughout the whole mapping area by an experienced international soil mapper (Dr. Reinhard Hartwich, former member of BGR, and co-author of the 1998 Manual of Procedures). The methodology is extensively described in the Explanatory Notes (German), and in the revised Manual of Procedures which is expected to be completed soon. It is highly recommended to apply and interpret the map using the map comments and descriptions as provided in the explanatory notes (German: Hartwich et al. 2005; English: revision of the Manual of Procedures, initial version: Finke et al. 2001).

Soil Regions of the European Union and Adjacent Countries 1:5,000,000

The map of the "Soil Regions of the European Union and Adjacent Countries 1:5,000,000 (Version 2.0)" is published by the Federal Institute of Geosciences and Natural Resources (BGR), in partnership with the Joint Research Center (JRC, Ispra). The soil regions map is intended to support the current national mapping activities towards a European 1:250,000 datbase by stratifying similar regional soil associations into a hierarchical concept. Only by stratification, the complexity of soils can be systematically structured so that the complex 1:250,000 legend can be handled in cross-national and contintental-level applications. Soil regions are natural, cross-regional soil geographical units which perform the highest spatial and content-based aggregation of European soils. They represent the frame conditions for soil development at the landscape level. The soil regions are presented at scale 1:5,000,000. Thus, its borders are highly generalized. Because of its low resolution, the map units absorb atypical soils and associations of soils, which are only described in higher resolution soil maps. The delineation of the soil regions is expected to be refined (and probably improved by its content) during the actual 1:250,000 mapping process. Thus, updating can be expected in the future. Currently, the soil regions map is the only graphical soil representation in Europe which has been developed using fully comparable and harmonized basic data at the continental level (climate, hydrography, relief, geology, vegetation): the interpretation of this input data, and the utilization of expert knowledge (including the interpretation of regional soil maps) has been done using one common methodology, developed and applied consistently throughout the whole mapping area by an experienced international soil mapper (Dr. Reinhard Hartwich, former member of BGR, and co-author of the 1998 Manual of Procedures). The methodology is extensively described in the Explanatory Notes (German), and in the revised Manual of Procedures which is expected to be completed soon. It is highly recommended to apply and interpret the map using the map comments and descriptions as provided in the explanatory notes (German: Hartwich et al. 2005; English: revision of the Manual of Procedures, initial version: Finke et al. 2001).

What Makes an Ideal Global Stocktake? A Functional Analysis

Many hope that the Global Stocktake under the Paris Agreement can become a catalyst for increased mitigation ambition over time. Based on different theories of change, this paper outlines four governance functions for the Global Stocktake. It can contribute to the Paris Agreement as a pacemaker (stimulating and synchronizing policy processes across governance levels), by ensuring accountability of Parties, by enhancing ambition through benchmarks for action and transformative learning, and by reiterating and refining the guidance and signal provided from the Paris Agreement. The paper further outlines process- and information-related preconditions that would enable an ideal Global Stocktake. Veröffentlicht in Climate Change | 22/2018.

Zu viel Dünger: Trinkwasser könnte teurer werden

Preissteigerung bis zu 45 Prozent erwartet Trinkwasser könnte in etlichen Regionen Deutschlands in Zukunft spürbar teurer werden. Grund ist die hohe Belastung des Grundwassers mit Nitrat. Über 27 Prozent der Grundwasserkörper überschreiten derzeit den Grenzwert von 50 mg/l. Wenn die Nitrateinträge dort nicht bald sinken, müssen betroffene Wasserversorger zu teuren Aufbereitungsmethoden greifen, um das Rohwasser von Nitrat zu reinigen. Einer aktuellen Studie des Umweltbundesamtes (UBA) zufolge kann dies die Trinkwasserkosten um 55 bis 76 Cent pro Kubikmeter erhöhen. Das entspricht einer Preissteigerung von 32 bis 45 Prozent. Eine vierköpfige Familie müsste dann bis zu 134 € im Jahr mehr bezahlen. Maria Krautzberger, Präsidentin des ⁠ UBA ⁠: „Mit den Neuregelungen in der Düngeverordnung wurden lange überfällige Schritte eingeleitet, die hoffentlich die Belastungen so weit senken, dass den Trinkwasserkunden die teure Aufbereitung erspart bleibt. Wichtig sind jetzt eine konsequente Umsetzung und verstärkte Kontrollen in den betroffenen Regionen. Falls sich diese Belastungen nicht verringern, müssten weitere und strengere Auflagen für die Landwirtschaft erfolgen.“ Gerade in Gebieten mit landwirtschaftlich intensiv genutzten Flächen ist das Grundwasser häufig durch zu viel Stickstoff belastet. Grund sind die auf den Feldern aufgebrachten Gülle und Mist aus der intensiven Tierhaltung oder Mineraldünger für beispielsweise Obst- und Gemüseanbau. Wasserversorger versuchen bereits heute, das Wasser mit unterschiedlichen Maßnahmen zu schützen, indem sie die darüber liegenden Flächen selbst pachten, Brunnen verlagern oder belastetes mit unbelastetem Wasser mischen. Auch diese Kosten fließen bereits heute in den Trinkwasserpreis mit ein. Doch derartige Maßnahmen werden in Zukunft in hochbelasteten Regionen nicht ausreichen, um den Nitratwert im Trinkwasser niedrig zu halten. Die UBA-Studie hat dies mit Daten von und in Kooperation mit drei großen Wasserversorgern untersucht: OOWV (Oldenburgisch-Ostfriesischer Wasserverband), Rheinenergie und RWW (Rheinisch-Westfälische Wasserwerksgesellschaft). Ergebnis: In einigen Gebieten könnte bald der Fall eintreten, dass das Wasser zusätzlich gereinigt werden muss. Dazu gibt es unterschiedliche Verfahren: Elektrodialyse, Umkehrosmose, biologische Denitrifikation oder das CARIX-Verfahren. Welches Verfahren zur Anwendung kommen kann, wird durch lokale Faktoren wie der Wasserhärte oder der notwendigen Vor- oder Nachbehandlung des Wassers bestimmt. Die Gesamtkosten für die Reinigung hängen neben der Art des Verfahrens auch noch ab von der konkreten Belastungssituation vor Ort, dem zu erreichenden Nitratwert, bis zu dem die Verunreinigungen gemindert werden sollen (Zielwert), und der Menge des aufzubereitenden Wassers. In jedem Falle bedeuten die Verfahren mögliche berechnete Mehrkosten von bis zu 76 Cent pro Kubikmeter für die Wasserkunden: diese müssen also für die Überdüngung in ihrer Region bezahlen. Die Studie rechnet zudem aus, wieviel die Reinigung von mit Nitrat belastetem Grundwasser in Deutschland insgesamt kosten kann: zwischen 580 und 767 Millionen Euro pro Jahr. Zum Vergleich: Maßnahmen der novellierten Düngeverordnung kosten laut Bundeslandwirtschaftsministerium die Landwirtschaft bis zu 111,7 Millionen Euro pro Jahr, also nur einen Bruchteil dessen, den die betroffenen Trinkwasserkunden zu bezahlen hätten. Dies zeigt erneut: Vorsorge ist billiger als Reparatur. Diese Maßnahmen helfen nicht nur, Nitrateinträge zu reduzieren und die Kosten für die Aufbereitung zu senken. Daneben haben sie sogar noch viele weitere positive Auswirkungen auf die Umwelt, wie den Erhalt der Artenvielfalt. Zur novellierten Düngegesetzgebung gehört neben dem Düngegesetz und die geplante Einführung einer Stoffstrombilanzverordnung auch die Düngeverordnung, die nach einem langjährigen Prozess umfangreich überarbeitet und im Frühjahr 2017 verabschiedet wurde.

Bootsrumpf-Anstriche – ein Problem für unsere Gewässer

Kupfereintrag aus Antifouling-Anstrichen sollte reduziert werden Deutsche Oberflächengewässer werden nach einer aktuellen Schätzung jährlich mit circa 70 Tonnen Kupfer aus Antifouling-Anstrichen von Sportbooten belastet. Um vor unerwünschtem Bewuchs durch etwa Algen oder Muscheln zu schützen, werden häufig biozidhaltige Anstriche aufgetragen. Kupfer ist das am häufigsten eingesetzte Biozid in Antifouling-Anstrichen. Die freigesetzte Kupfermenge entspricht rund 19 Prozent der gesamten Kupfereinträge in deutsche Oberflächengewässer und wirkt dort ökotoxisch auf Bakterien, Algen, Flusskrebse und Fische. Das Umweltbundesamt (UBA) rät zu alternativen Hartbeschichtungen und mechanischer Reinigung mit zum Beispiel Unterwasserbürsten sowie geeigneten Anstrichen ohne Biozide. Regionale Differenzierungen und Dokumentationen bei der Anwendung, Beratung der Anwendenden sowie amtliche Kontrollen der Kupfergehalte können die Kupferbelastungen reduzieren. Umweltqualitätsnormen der Oberflächengewässerverordnung (OGewV), die den guten, ökologischen Zustand von Oberflächengewässern beschreiben, werden für Kupfer an elf Prozent der offiziellen Messstellen überschritten. Kupferhaltige Anstriche werden häufig bei Sportbooten eingesetzt. Daher sind vor allem hier Maßnahmen sinnvoll, um die Gewässerbelastungen zu reduzieren. Wie das geht, zeigen Beispiele aus Skandinavien. So sind in Schweden für weite Teile der Ostsee nur Produkte mit reduziertem Kupferanteil zugelassen und für den Binnenbereich ist jeglicher Biozideinsatz in Antifouling-Anstrichen verboten. Diese regionalen Regelungen könnten auch für Deutschland ein Vorbild sein. Bisher jedoch sind umweltschädliche, biozidhaltige Antifouling-Anstriche nur in einer kleinen Region in Schleswig-Holstein verboten. Solche regionalen Differenzierungen sind nur schwer bei der Produktzulassung nach EU-Biozid-Verordnung umsetzbar. Deshalb sollte Deutschland hier – ebenso wie beispielsweise Schweden – eigene Regelungen finden, die alle Zuständigen im Bereich des Bundes, der Länder und auch die Hersteller von Antifouling-Anstrichen, die Sportbootsverbände, die Hafenbetreiber und die Bootsbesitzenden einbinden. In Binnengewässern ist der Bootsrumpfbewuchs geringer, weshalb auf biozidhaltige Produkte ganz verzichtet werden sollte. Bootsrümpfe können beispielsweise mit Hartbeschichtungen versehen werden, die sich dann mit Unterwasserbürsten reinigen lassen. In der Ostsee sind Anstriche mit niedrigeren Kupfergehalten und solche, die weniger Kupfer ins Wasser abgeben, ausreichend. In der Nordsee kann dagegen auf Antifouling-Anstriche nicht verzichtet werden. Entsprechend der unterschiedlichen, regionalen Anforderungen sollten die Anstriche durch die Hersteller übergreifend nach einem dreistufigen Ampelsystem (Nordsee, Ostsee, Binnengewässer) gekennzeichnet werden, um die Auswahl für die Anwendenden zu erleichtern. Diese sollten die Erneuerung der Anstriche in ihren Fahrten- oder Logbüchern dokumentieren. Mit transportablen Handgeräten ist die amtliche Kontrolle der Kupfergehalte auf den Bootsrümpfen stichprobenartig möglich. Ein neues Hintergrundpapier des Umweltbundesamtes informiert rund um Antifouling-Anstriche und Stoffeinträge und gibt Empfehlungen für einen umweltfreundlichen Einsatz.

Relevanz der gewerblichen Textil- und Geschirrreinigung am Eintrag von Phosphat und anderen Phosphorverbindungen (P) in das Abwasser

Der vom Umweltbundesamt beauftragte Forschungsbericht hatte zum Ziel, die Relevanz der gewerblichen Textil- und Geschirrreinigung im Hinblick auf den Eintrag von Phosphat und anderen Phosphorverbindungen (P) in das Abwasser und damit auf die ⁠ Gewässergüte ⁠ zu untersuchen. In einem ersten Schritt wird ein Überblick über die verschiedenen technischen Verfahren der gewerblichen Textil- und Geschirrreinigung gegeben und der Frage nachgegangen, wo bereits heute auf Phosphat verzichtet werden kann bzw. wo Phosphat für eine optimale Reinigung unter Beachtung von Hygiene, Energie- und Wasserverbrauch unerlässlich ist. Ausgehend von den in der gewerblichen Textil- und Geschirrreinigung eingesetzten Phosphor-Mengen wird eine Abschätzung der Auswirkung einer Reduktion des Phosphor-Einsatzes im gewerblichen Bereich auf die Gewässergüte vorgenommen. Veröffentlicht in Texte | 98/2021.

Leitfaden zur umweltfreundlichen öffentlichen Beschaffung: System Stoffhandtuchrollen im Stoffhandtuchspender

Zum Abtrocknen und Nachreinigen der Hände nach der Handwäsche in öffentlichen Einrichtungen bieten sich bei Betrachtung der Hygiene, der Gebrauchstauglichkeit und unter Umweltgesichtspunkten Stoffhandtuchrollen an. Die Kriterien des Leitfadens zur umweltfreundlichen öffentlichen Beschaffung beziehen sich unter anderem auf eine lange Lebensdauer (80 bis 100 Umläufe), hygienische Eigenschaften und Weiterverwendung der Stoffhandtuchrollen (z. B. als Putztücher). Zudem werden hohe Anforderungen an das Reinigungsverfahren in Wäschereien gestellt. Der Leitfaden basiert auf den Kriterien des Umweltzeichens Blauer Engel für das System Stoffhandtuchrollen im Stoffhandtuchspender (DE-UZ 77, Ausgabe Januar 2021). Veröffentlicht in Leitfäden und Handbücher.

Markt für Blei

technologyComment of gold mine operation and refining (SE): OPEN PIT MINING: The ore is mined in four steps: drilling, blasting, loading and hauling. In the case of a surface mine, a pattern of holes is drilled in the pit and filled with explosives. The explosives are detonated in order to break up the ground so large shovels or front-end loaders can load it into haul trucks. ORE AND WASTE HAULAGE: The haul trucks transport the ore to various areas for processing. The grade and type of ore determine the processing method used. Higher-grade ores are taken to a mill. Lower grade ores are taken to leach pads. Some ores may be stockpiled for later processing. HEAP LEACHING: The ore is crushed or placed directly on lined leach pads where a dilute cyanide solution is applied to the surface of the heap. The solution percolates down through the ore, where it leaches the gold and flows to a central collection location. The solution is recovered in this closed system. The pregnant leach solution is fed to electrowinning cells and undergoes the same steps as described below from Electro-winning. ORE PROCESSING: Milling: The ore is fed into a series of grinding mills where steel balls grind the ore to a fine slurry or powder. Oxidization and leaching: Some types of ore require further processing before gold is recovered. In this case, the slurry is pressure-oxidized in an autoclave before going to the leaching tanks or a dry powder is fed through a roaster in which it is oxidized using heat before being sent to the leaching tanks as a slurry. The slurry is thickened and runs through a series of leaching tanks. The gold in the slurry adheres to carbon in the tanks. Stripping: The carbon is then moved into a stripping vessel where the gold is removed from the carbon by pumping a hot caustic solution through the carbon. The carbon is later recycled. Electro-winning: The gold-bearing solution is pumped through electro-winning cells or through a zinc precipitation circuit where the gold is recovered from the solution. Smelting: The gold is then melted in a furnace at about 1’064°C and poured into moulds, creating doré bars. Doré bars are unrefined gold bullion bars containing between 60% and 95% gold. References: Newmont (2004) How gold is mined. Newmont. Retrieved from http://www.newmont.com/en/gold/howmined/index.asp technologyComment of primary lead production from concentrate (GLO): There are two basic pyrometallurgical processes available for the production of lead from lead or mixed lead-zinc-sulphide concentrates: sinter oxidation / blast furnace reduction route or Direct Smelting Reduction Processes. Both processes are followed by a refining step to produce the final product with the required purity, and may also be used for concentrates mixed with secondary raw materials. SINTER OXIDATION / BLAST FURNACE REDUCTION: The sinter oxidation / blast furnace reduction involves two steps: 1) A sintering oxidative roast to remove sulphur with production of PbO; and 2) Blast furnace reduction of the sinter product. The objective of sintering lead concentrates is to remove as much sulphur as possible from the galena and the accompanying iron, zinc, and copper sulphides, while producing lump agglomerate with appropriate properties for subsequent reduction in the blast furnace (a type of a shaft furnace). As raw material feed, lead concentrates are blended with recycled sinter fines, secondary material and other process materials and pelletised in rotating drums. Pellets are fed onto sinter machine and ignited. The burning pellets are conveyed over a series of wind-boxes through which air is blown. Sulphur is oxidised to sulphur dioxide and the reaction generates enough heat to fuse and agglomerate the pellets. Sinter is charged to the blast furnace with metallurgical coke. Air and/or oxygen enriched air is injected and reacts with the coke to produce carbon monoxide. This generates sufficient heat to melt the charge. The gangue content of the furnace charge combines with the added fluxes or reagents to form a slag. For smelting bulk lead-zinc-concentrates and secondary material, frequently the Imperial Smelting Furnace is used. Here, hot sinter and pre-heated coke as well as hot briquettes are charged. Hot air is injected. The reduction of the metal oxides not only produces lead and slag but also zinc, which is volatile at the furnace operating temperature and passes out of the ISF with the furnace off-gases. The gases also contain some cadmium and lead. The furnace gases pass through a splash condenser in which a shower of molten lead quenches them and the metals are absorbed into the liquid lead, the zinc is refined by distillation. DIRECT SMELTING REDUCTION: The Direct Smelting Reduction Process does not carry out the sintering stage separately. Lead sulphide concentrates and secondary materials are charged directly to a furnace and are then melted and oxidised. Sulphur dioxide is formed and is collected, cleaned and converted to sulphuric acid. Carbon (coke or gas) and fluxing agents are added to the molten charge and lead oxide is reduced to lead, a slag is formed. Some zinc and cadmium are “fumed” off in the furnace, their oxides are captured in the abatement plant and recovered. Several processes are used for direct smelting of lead concentrates and some secondary material to produce crude lead and slag. Bath smelting processes are used: the ISA Smelt/Ausmelt furnaces (sometimes in combination with blast furnaces), Kaldo (TBRC) and QSL integrated processes are used in EU and Worldwide. The Kivcet integrated process is also used and is a flash smelting process. The ISA Smelt/Ausmelt furnaces and the QSL take moist, pelletised feed and the Kaldo and Kivcet use dried feed. REFINING: Lead bullion may contain varying amounts of copper, silver, bismuth, antimony, arsenic and tin. Lead recovered from secondary sources may contain similar impurities, but generally antimony and calcium dominate. There are two methods of refining crude lead: electrolytic refining and pyrometallurgical refining. Electrolytic refining uses anodes of de-copperised lead bullion and starter cathodes of pure lead. This is a high-cost process and is used infrequently. A pyrometallurgical refinery consists of a series of kettles, which are indirectly heated by oil or gas. Over a series of separation processes impurities and metal values are separated from the lead bouillon. Overall waste: The production of metals is related to the generation of several by-products, residues and wastes, which are also listed in the European Waste Catalogue (Council Decision 94/3/EEC). The ISF or direct smelting furnaces also are significant sources of solid slag. This slag has been subjected to high temperatures and generally contains low levels of leachable metals, consequently it may be used in construction. Solid residues also arise as the result of the treatment of liquid effluents. The main waste stream is gypsum waste (CaSO4) and metal hydroxides that are produced at the wastewater neutralisation plant. These wastes are considered to be a cross-media effect of these treatment techniques but many are recycled to pyrometallurgical process to recover the metals. Dust or sludge from the treatment of gases are used as raw materials for the production of other metals such as Ge, Ga, In and As, etc or can be returned to the smelter or into the leach circuit for the recovery of lead and zinc. Hg/Se residues arise at the pre-treatment of mercury or selenium streams from the gas cleaning stage. This solid waste stream amounts to approximately 40 - 120 t/y in a typical plant. Hg and Se can be recovered from these residues depending on the market for these metals. Overall emissions: The main emissions to air from zinc and lead production are sulphur dioxide, other sulphur compounds and acid mists; nitrogen oxides and other nitrogen compounds, metals and their compounds; dust; VOC and dioxins. Other pollutants are considered to be of negligible importance for the industry, partly because they are not present in the production process and partly because they are immediately neutralised (e.g. chlorine) or occur in very low concentrations. Emissions are to a large extent bound to dust (except cadmium, arsenic and mercury that can be present in the vapour phase). Metals and their compounds and materials in suspension are the main pollutants emitted to water. The metals concerned are Zn, Cd, Pb, Hg, Se, Cu, Ni, As, Co and Cr. Other significant substances are fluorides, chlorides and sulphates. Wastewater from the gas cleaning of the smelter and fluid-bed roasting stages are the most important sources. References: Sutherland C. A., Milner E. F., Kerby R. C., Teindl H. and Melin A. (1997) Lead. In: Ullmann's encyclopedia of industrial chemistry (ed. Anonymous). 5th edition on CD-ROM Edition. Wiley & Sons, London. IPPC (2001) Integrated Pollution Prevention and Control (IPPC); Reference Document on Best Available Techniques in the Non Ferrous Metals Industries. European Commission. Retrieved from http://www.jrc.es/pub/english.cgi/ 0/733169 technologyComment of primary zinc production from concentrate (RoW): The technological representativeness of this dataset is considered to be high as smelting methods for zinc are consistent in all regions. Refined zinc produced pyro-metallurgically represents less than 5% of global zinc production and less than 2% of this dataset. Electrometallurgical Smelting The main unit processes for electrometallurgical zinc smelting are roasting, leaching, purification, electrolysis, and melting. In both electrometallurgical and pyro-metallurgical zinc production routes, the first step is to remove the sulfur from the concentrate. Roasting or sintering achieves this. The concentrate is heated in a furnace with operating temperature above 900 °C (exothermic, autogenous process) to convert the zinc sulfide to calcine (zinc oxide). Simultaneously, sulfur reacts with oxygen to produce sulfur dioxide, which is subsequently converted to sulfuric acid in acid plants, usually located with zinc-smelting facilities. During the leaching process, the calcine is dissolved in dilute sulfuric acid solution (re-circulated back from the electrolysis cells) to produce aqueous zinc sulfate solution. The iron impurities dissolve as well and are precipitated out as jarosite or goethite in the presence of calcine and possibly ammonia. Jarosite and goethite are usually disposed of in tailing ponds. Adding zinc dust to the zinc sulfate solution facilitates purification. The purification of leachate leads to precipitation of cadmium, copper, and cobalt as metals. In electrolysis, the purified solution is electrolyzed between lead alloy anodes and aluminum cathodes. The high-purity zinc deposited on aluminum cathodes is stripped off, dried, melted, and cast into SHG zinc ingots (99.99 % zinc). Pyro-metallurgical Smelting The pyro-metallurgical smelting process is based on the reduction of zinc and lead oxides into metal with carbon in an imperial smelting furnace. The sinter, along with pre-heated coke, is charged from the top of the furnace and injected from below with pre-heated air. This ensures that temperature in the center of the furnace remains in the range of 1000-1500 °C. The coke is converted to carbon monoxide, and zinc and lead oxides are reduced to metallic zinc and lead. The liquid lead bullion is collected at the bottom of the furnace along with other metal impurities (copper, silver, and gold). Zinc in vapor form is collected from the top of the furnace along with other gases. Zinc vapor is then condensed into liquid zinc. The lead and cadmium impurities in zinc bullion are removed through a distillation process. The imperial smelting process is an energy-intensive process and produces zinc of lower purity than the electrometallurgical process. technologyComment of treatment of electronics scrap, metals recovery in copper smelter (SE, RoW): Conversion of Copper in a Kaldo Converter and treatment in converter aisle. technologyComment of treatment of scrap lead acid battery, remelting (RoW): The referred operation uses a shaft furnace with post combustion, which is the usual technology for secondary smelters. technologyComment of treatment of scrap lead acid battery, remelting (RER): The referred operation uses a shaft furnace with post combustion, which is the usual technology for secondary smelters. Typically this technology produces 5000 t / a sulphuric acid (15% concentration), 25’000 t lead bullion (98% Pb), 1200 t / a slags (1% Pb) and 3000 t / a raw lead matte (10% Pb) to be shipped to primary smelters. Overall Pb yield is typically 98.8% at the plant level and 99.8% after reworking the matte. The operation treats junk batteries and plates but also lead cable sheathing, drosses and sludges, leaded glass and balancing weights. From this feed it manufactures mainly antimonial lead up to 10% Sb, calcium-aluminium lead alloys with or without tin and soft lead with low and high copper content. All these products are the result of a refining and alloying step to meet the compliance with the designations desired. The following by products are reused in the process: fine dust, slag, and sulfuric acid. References: Quirijnen L. (1999) How to implement efficient local lead-acid battery recycling. In: Journal of Power Sources, 78(1-2), pp. 267-269.

Markt für Silber

technologyComment of gold mine operation and refining (SE): OPEN PIT MINING: The ore is mined in four steps: drilling, blasting, loading and hauling. In the case of a surface mine, a pattern of holes is drilled in the pit and filled with explosives. The explosives are detonated in order to break up the ground so large shovels or front-end loaders can load it into haul trucks. ORE AND WASTE HAULAGE: The haul trucks transport the ore to various areas for processing. The grade and type of ore determine the processing method used. Higher-grade ores are taken to a mill. Lower grade ores are taken to leach pads. Some ores may be stockpiled for later processing. HEAP LEACHING: The ore is crushed or placed directly on lined leach pads where a dilute cyanide solution is applied to the surface of the heap. The solution percolates down through the ore, where it leaches the gold and flows to a central collection location. The solution is recovered in this closed system. The pregnant leach solution is fed to electrowinning cells and undergoes the same steps as described below from Electro-winning. ORE PROCESSING: Milling: The ore is fed into a series of grinding mills where steel balls grind the ore to a fine slurry or powder. Oxidization and leaching: Some types of ore require further processing before gold is recovered. In this case, the slurry is pressure-oxidized in an autoclave before going to the leaching tanks or a dry powder is fed through a roaster in which it is oxidized using heat before being sent to the leaching tanks as a slurry. The slurry is thickened and runs through a series of leaching tanks. The gold in the slurry adheres to carbon in the tanks. Stripping: The carbon is then moved into a stripping vessel where the gold is removed from the carbon by pumping a hot caustic solution through the carbon. The carbon is later recycled. Electro-winning: The gold-bearing solution is pumped through electro-winning cells or through a zinc precipitation circuit where the gold is recovered from the solution. Smelting: The gold is then melted in a furnace at about 1’064°C and poured into moulds, creating doré bars. Doré bars are unrefined gold bullion bars containing between 60% and 95% gold. References: Newmont (2004) How gold is mined. Newmont. Retrieved from http://www.newmont.com/en/gold/howmined/index.asp technologyComment of gold-silver mine operation with refinery (PG): OPEN PIT MINING: The ore is mined in four steps: drilling, blasting, loading and hauling. In the case of a surface mine, a pattern of holes is drilled in the pit and filled with explosives. The explosives are detonated in order to break up the ground so large shovels or front-end loaders can load it into haul trucks. ORE AND WASTE HAULAGE: The haul trucks transport the ore to various areas for processing. The grade and type of ore determine the processing method used. Higher-grade ores are taken to a mill. Lower grade ores are taken to leach pads. Some ores may be stockpiled for later processing. HEAP LEACHING: The recovery processes of the Misima Mine are cyanide leach and carbon in pulp (CIP). The ore is crushed or placed directly on lined leach pads where a dilute cyanide solution is applied to the surface of the heap. The solution percolates down through the ore, where it leaches the gold and flows to a central collection location. The solution is recovered in this closed system. The pregnant leach solution is fed to electrowinning cells and undergoes the same steps as described below from Electro-winning. ORE PROCESSING: Milling: The ore is fed into a series of grinding mills where steel balls grind the ore to a fine slurry or powder. Oxidization and leaching: The recovery process in the Porgera Mine is pressure oxidation and cyanide leach. The slurry is pressure-oxidized in an autoclave before going to the leaching tanks or a dry powder is fed through a roaster in which it is oxidized using heat before being sent to the leaching tanks as a slurry. The slurry is thickened and runs through a series of leaching tanks. The gold in the slurry adheres to carbon in the tanks. Stripping: The carbon is then moved into a stripping vessel where the gold is removed from the carbon by pumping a hot caustic solution through the carbon. The carbon is later recycled. Electro-winning: The gold-bearing solution is pumped through electro-winning cells or through a zinc precipitation circuit where the gold is recovered from the solution. Smelting: The gold is then melted in a furnace at about 1’064°C and poured into moulds, creating doré bars. Doré bars are unrefined gold bullion bars containing between 60% and 95% gold. WATER SUPPLY: For Misima Mine, process water is supplied from pit dewatering bores and in-pit water. Potable water is sourced from boreholes in the coastal limestone. For Porgera Mine, the main water supply of the mine is the Waile Creek Dam, located approximately 7 kilometres from the mine. The reservoir has a capacity of approximately 717, 000 m3 of water. Water for the grinding circuit is also extracted from Kogai Creek, which is located adjacent to the grinding circuit. The mine operates four water treatment plants for potable water and five sewage treatment plants. ENERGY SUPPLY: For Misima Mine, electricity is produced by the mine on site or with own power generators, from diesel and heavy fuel oil. For Porgera Mine, electricity is produced by the mine on site. Assumed with Mobius / Wohlwill electrolysis. Porgera's principal source of power is supplied by a 73-kilometre transmission line from the gas fired and PJV-owned Hides Power Station. The station has a total output of 62 megawatts (“MW”). A back up diesel power station is located at the mine and has an output of 13MW. The average power requirement of the mine is about 60 MW. For both Misima and Porgera Mines, an 18 MW diesel fired power station supplies electrical power. Diesel was used in the station due to the unavailability of previously supplied heavy fuel oil. technologyComment of gold-silver mine operation with refinery (CA-QC): One of the modelled mine is an open-pit mine and the two others are underground. technologyComment of gold-silver mine operation with refinery (RoW): The mining of ore from open pit mines is considered. technologyComment of primary zinc production from concentrate (RoW): The technological representativeness of this dataset is considered to be high as smelting methods for zinc are consistent in all regions. Refined zinc produced pyro-metallurgically represents less than 5% of global zinc production and less than 2% of this dataset. Electrometallurgical Smelting The main unit processes for electrometallurgical zinc smelting are roasting, leaching, purification, electrolysis, and melting. In both electrometallurgical and pyro-metallurgical zinc production routes, the first step is to remove the sulfur from the concentrate. Roasting or sintering achieves this. The concentrate is heated in a furnace with operating temperature above 900 °C (exothermic, autogenous process) to convert the zinc sulfide to calcine (zinc oxide). Simultaneously, sulfur reacts with oxygen to produce sulfur dioxide, which is subsequently converted to sulfuric acid in acid plants, usually located with zinc-smelting facilities. During the leaching process, the calcine is dissolved in dilute sulfuric acid solution (re-circulated back from the electrolysis cells) to produce aqueous zinc sulfate solution. The iron impurities dissolve as well and are precipitated out as jarosite or goethite in the presence of calcine and possibly ammonia. Jarosite and goethite are usually disposed of in tailing ponds. Adding zinc dust to the zinc sulfate solution facilitates purification. The purification of leachate leads to precipitation of cadmium, copper, and cobalt as metals. In electrolysis, the purified solution is electrolyzed between lead alloy anodes and aluminum cathodes. The high-purity zinc deposited on aluminum cathodes is stripped off, dried, melted, and cast into SHG zinc ingots (99.99 % zinc). Pyro-metallurgical Smelting The pyro-metallurgical smelting process is based on the reduction of zinc and lead oxides into metal with carbon in an imperial smelting furnace. The sinter, along with pre-heated coke, is charged from the top of the furnace and injected from below with pre-heated air. This ensures that temperature in the center of the furnace remains in the range of 1000-1500 °C. The coke is converted to carbon monoxide, and zinc and lead oxides are reduced to metallic zinc and lead. The liquid lead bullion is collected at the bottom of the furnace along with other metal impurities (copper, silver, and gold). Zinc in vapor form is collected from the top of the furnace along with other gases. Zinc vapor is then condensed into liquid zinc. The lead and cadmium impurities in zinc bullion are removed through a distillation process. The imperial smelting process is an energy-intensive process and produces zinc of lower purity than the electrometallurgical process. technologyComment of processing of anode slime from electrorefining of copper, anode (GLO): Based on typical current technology. Anode slime treatment by pressure leaching and top blown rotary converter. Production of Silver by Möbius Electrolysis, Gold by Wohlwill electrolysis, copper telluride cement and crude selenium to further processing. technologyComment of silver-gold mine operation with refinery (CL): OPEN PIT MINING: The ore is mined in four steps: drilling, blasting, loading and hauling. In the case of a surface mine, a pattern of holes is drilled in the pit and filled with explosives. The explosives are detonated in order to break up the ground so large shovels or front-end loaders can load it into haul trucks. BENEFICIATION: The processing plant consists of primary crushing, a pre-crushing circuit, (semi autogenous ball mill crushing) grinding, leaching, filtering and washing, Merrill-Crowe plant and doré refinery. The Merrill-Crowe metal recovery circuit is better than a carbon-in-pulp system for the high-grade silver material. Tailings are filtered to recover excess water as well as residual cyanide and metals. A dry tailings disposal system was preferred to a conventional wet tailings impoundment because of site-specific environmental considerations. technologyComment of silver-gold mine operation with refinery (RoW): Refinement is estimated with electrolysis-data. technologyComment of treatment of crust from Parkes process for lead production (GLO): Processing of Parkes desilvering crust by hot pressing, dezincing (vacuum distillation), cupellation of lead and moebius electrolysis (electrowinning) technologyComment of treatment of precious metal from electronics scrap, in anode slime, precious metal extraction (SE, RoW): Anode slime treatment by pressure leaching and top blown rotary converter. Production of Silver by Möbius Electrolysis, Gold by Wohlwill electrolysis, Palladium to further processing technologyComment of treatment of waste x-ray film (GLO): None

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technologyComment of gold mine operation and refining (SE): OPEN PIT MINING: The ore is mined in four steps: drilling, blasting, loading and hauling. In the case of a surface mine, a pattern of holes is drilled in the pit and filled with explosives. The explosives are detonated in order to break up the ground so large shovels or front-end loaders can load it into haul trucks. ORE AND WASTE HAULAGE: The haul trucks transport the ore to various areas for processing. The grade and type of ore determine the processing method used. Higher-grade ores are taken to a mill. Lower grade ores are taken to leach pads. Some ores may be stockpiled for later processing. HEAP LEACHING: The ore is crushed or placed directly on lined leach pads where a dilute cyanide solution is applied to the surface of the heap. The solution percolates down through the ore, where it leaches the gold and flows to a central collection location. The solution is recovered in this closed system. The pregnant leach solution is fed to electrowinning cells and undergoes the same steps as described below from Electro-winning. ORE PROCESSING: Milling: The ore is fed into a series of grinding mills where steel balls grind the ore to a fine slurry or powder. Oxidization and leaching: Some types of ore require further processing before gold is recovered. In this case, the slurry is pressure-oxidized in an autoclave before going to the leaching tanks or a dry powder is fed through a roaster in which it is oxidized using heat before being sent to the leaching tanks as a slurry. The slurry is thickened and runs through a series of leaching tanks. The gold in the slurry adheres to carbon in the tanks. Stripping: The carbon is then moved into a stripping vessel where the gold is removed from the carbon by pumping a hot caustic solution through the carbon. The carbon is later recycled. Electro-winning: The gold-bearing solution is pumped through electro-winning cells or through a zinc precipitation circuit where the gold is recovered from the solution. Smelting: The gold is then melted in a furnace at about 1’064°C and poured into moulds, creating doré bars. Doré bars are unrefined gold bullion bars containing between 60% and 95% gold. References: Newmont (2004) How gold is mined. Newmont. Retrieved from http://www.newmont.com/en/gold/howmined/index.asp technologyComment of primary zinc production from concentrate (CA-QC): Hydrometallurgical process Sulphide concentrates are roasted first in fluidized bed roasters to produce zinc oxide (calcine) and sulphur dioxide. Roasting is an exothermic process and no additional fuel is used to sustain the reaction, the heat generated is recovered to produce steam. Calcine is then sent to the leaching step. Roaster gases are treated in hot electrostatics precipitators to remove dust. The remaining dust and volatile metals such as mercury and selenium are removed in the wet section of the acid plant through a cooling tour, a mist precipitator and a mercury tower (Boliden mercury removal processs). The sulphur dioxide is then converted to sulphuric acid in a conventional recovery system (converted and absorbing tower). Leaching of the calcine is carried out in a number of successive stages using a gradually increasing strength of hot sulphuric acid. The initial stages dissolve the major part of the zinc oxide and the other stages dissolve the zinc ferrite (ZnO.Fe2O3) and convert iron into Jarosite (sodium Jarosite). Zinc sulfate (ZnSO4) entering the electrolysis stage produce electrolyte (H2SO4) that is returned to leaching plant. Other metals are also dissolved during the process and are removed after leaching. Iron is the major impurity, which is precipitated in the form of Jarosite. Overall waste: The production of metals is related to the generation of several by-products, residues and wastes. Relatively large quantities of iron based solids, depending on the iron content, are generated by the leaching process (6.14E-1 kg Jarosite/kg zinc). Cement is added to the Jarosite to produce Jarofix (an inert waste). Solid residues also arise as the result of the liquid effluents treatment. The main waste stream is gypsum (CaSO4) and metal hydroxides that are produced at the wastewater neutralization plant. Mercury and selenium residues arise from the weak acid bleed treatment from the acid plant. Selenium can be recovered from these residues depending on the market demand for this metal. Overall emissions: The emissions to air can either be stack emissions or fugitive emissions. Stack emissions are normally monitored continuously (SO2) or periodically (other emissions) and reported. The main emissions to air from zinc production are sulphur dioxide (SO2) and particulate matters including metals. Main emissions to water are metals and their compounds. The monitored metals are zinc, cadmium, lead, mercury, selenium, copper and arsenic. technologyComment of primary zinc production from concentrate (RoW): The technological representativeness of this dataset is considered to be high as smelting methods for zinc are consistent in all regions. Refined zinc produced pyro-metallurgically represents less than 5% of global zinc production and less than 2% of this dataset. Electrometallurgical Smelting The main unit processes for electrometallurgical zinc smelting are roasting, leaching, purification, electrolysis, and melting. In both electrometallurgical and pyro-metallurgical zinc production routes, the first step is to remove the sulfur from the concentrate. Roasting or sintering achieves this. The concentrate is heated in a furnace with operating temperature above 900 °C (exothermic, autogenous process) to convert the zinc sulfide to calcine (zinc oxide). Simultaneously, sulfur reacts with oxygen to produce sulfur dioxide, which is subsequently converted to sulfuric acid in acid plants, usually located with zinc-smelting facilities. During the leaching process, the calcine is dissolved in dilute sulfuric acid solution (re-circulated back from the electrolysis cells) to produce aqueous zinc sulfate solution. The iron impurities dissolve as well and are precipitated out as jarosite or goethite in the presence of calcine and possibly ammonia. Jarosite and goethite are usually disposed of in tailing ponds. Adding zinc dust to the zinc sulfate solution facilitates purification. The purification of leachate leads to precipitation of cadmium, copper, and cobalt as metals. In electrolysis, the purified solution is electrolyzed between lead alloy anodes and aluminum cathodes. The high-purity zinc deposited on aluminum cathodes is stripped off, dried, melted, and cast into SHG zinc ingots (99.99 % zinc). Pyro-metallurgical Smelting The pyro-metallurgical smelting process is based on the reduction of zinc and lead oxides into metal with carbon in an imperial smelting furnace. The sinter, along with pre-heated coke, is charged from the top of the furnace and injected from below with pre-heated air. This ensures that temperature in the center of the furnace remains in the range of 1000-1500 °C. The coke is converted to carbon monoxide, and zinc and lead oxides are reduced to metallic zinc and lead. The liquid lead bullion is collected at the bottom of the furnace along with other metal impurities (copper, silver, and gold). Zinc in vapor form is collected from the top of the furnace along with other gases. Zinc vapor is then condensed into liquid zinc. The lead and cadmium impurities in zinc bullion are removed through a distillation process. The imperial smelting process is an energy-intensive process and produces zinc of lower purity than the electrometallurgical process.

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