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 production (US): 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. UNDERGROUND MINING: Some ore bodies are more economically mined underground. In this case, a tunnel called an adit or a shaft is dug into the earth. Sort tunnels leading from the adit or shaft, called stopes, are dug to access the ore. The surface containing the ore, called a face, is drilled and loaded with explosives. Following blasting, the broken ore is loaded onto electric trucks and taken to the surface. Once mining is completed in a particular stope, it is backfilled with a cement compound. BENEFICIATION: Bald Mountain Mines: The ore treatment method is based on conventional heap leaching technology followed by carbon absorption. The loaded carbon is stripped and refined in the newly commissioned refinery on site. Water is supplied by wells located on the mine property. Grid power was brought to Bald Mountain Mine in 1996. For this purpose, one 27-kilometre 69 KVA power line was constructed from the Alligator Ridge Mine substation to the grid. Golden Sunlight Mines: The ore treatment plant is based on conventional carbon-in-pulp technology, with the addition of a Sand Tailings Retreatment (STR) gold recovery plant to recover gold that would otherwise be lost to tailings. The STR circuit removes the heavier gold bearing pyrite from the sand portion of the tailings by gravity separation. The gold is refined into doré at the mine. Tailing from the mill is discharged to an impoundment area where the solids are allowed to settle so the water can be reused. A cyanide recovery/destruction process was commissioned in 1998. It eliminates the hazard posed to wildlife at the tailings impoundment by lowering cyanide concentrations below 20 mg/l. Fresh water for ore processing, dust suppression, and fire control is supplied from the Jefferson Slough, which is an old natural channel of the Jefferson River. Ore processing also uses water pumped from the tailings impoundment. Pit water is treated in a facility located in the mill complex prior to disposal or for use in dust control. Drinking water is made available by filtering fresh water through an on-site treatment plant. Electric power is provided from a substation at the south property boundary. North-Western Energy supplies electricity the substation. Small diesel generators are used for emergency lighting. A natural gas pipeline supplies gas for heating buildings, a crusher, air scrubber, boiler, carbon reactivation kiln, and refining furnaces. Cortez Mine: Three different metallurgical processes are employed for the recovery of gold. The process used for a particular ore is determined based on grade and metallurgical character of that ore. Lower grade oxide ore is heap leached, while higher-grade non-refractory ore is treated in a conventional mill using cyanidation and a carbon-in-leach (“CIL”) process. When carbonaceous ore is processed by Barrick, it is first dry ground, and then oxidized in a circulating fluid bed roaster, followed by CIL recovery. In 2002 a new leach pad and process plant was commissioned; this plant is capable of processing 164 million tonnes of heap leach ore over the life of the asset. Heap leach ore production is hauled directly to heap leach pads for gold recovery. Water for process use is supplied from the open pit dewatering system. Approximately 90 litres per second of the pit dewatering volume is diverted for plant use. Electric power is supplied by Sierra Pacific Power Company (“SPPC”) through a 73 kilometre, 120 kV transmission line. A long-term agreement is in place with SPPC to provide power through the regulated power system. The average power requirement of the mine is about 160 GWh/year. REFINING: Wohlwill electrolysis. It is assumed that the gold doré-bars from both mines undergo the treatment of Wohlwill electrolysis. This process uses an electrolyte containing 2.5 mol/l of HCl and 2 mol/l of HAuCl4 acid. Electrolysis is carried out with agitation at 65 – 75 °C. The raw gold is intro-duced as cast anode plates. The cathodes, on which the pure gold is deposited, were for many years made of fine gold of 0.25 mm thickness. These have now largely been replaced by sheet titanium or tantalum cathodes, from which the thick layer of fine gold can be peeled off. In a typical electrolysis cell, gold anodes weighing 12 kg and having dimensions 280×230×12 mm (0.138 m2 surface) are used. Opposite to them are conductively connected cathode plates, arranged by two or three on a support rail. One cell normally contains five or six cathode units and four or five anodes. The maximum cell voltage [V] is 1.5 V and the maximum anodic current density [A] 1500 A/m2. The South African Rand refinery gives a specific gold production rate of 0.2 kg per hour Wohlwill electrolysis. Assuming a current efficiency of 95% the energy consumption is [V] x [A] / 0.2 [kg/h] = 1.63 kWh per kg gold refined. No emissions are assumed because of the purity and the high value of the material processed. The resulting sludge contains the PGM present in the electric scrap and is sold for further processing. OTHER MINES: Information about the technology used in the remaining mines is described in the References. WATER EMISSIONS: Water effluents are discharged into rivers. References: Auerswald D. A. and Radcliffe P. H. (2005) Process technology development at Rand Refinery. In: Minerals Engineering, 18(8), pp. 748-753, Online-Version under: http://dx.doi.org/10.1016/j.mineng.2005.03.011. Newmont (2004) How gold is mined. Newmont. Retrieved from http://www.newmont.com/en/gold/howmined/index.asp Renner H., Schlamp G., Hollmann D., Lüschow H. M., Rothaut J., Knödler A., Hecht C., Schlott M., Drieselmann R., Peter C. and Schiele R. (2002) Gold, Gold Alloys, and Gold Compounds. In: Ullmann's Encyclopedia of Industrial Chemistry. Online version, posting date: September 15, 2000 Edition. Wiley-Interscience, Online-Version under: http://dx.doi.org/10.1002/14356007.a12_ 499. Barrick (2006b) Environment: Performance Tables from http://www.barrick. com/Default.aspx?SectionID=8906c4bd-4ee4-4f15-bf1b-565e357c01e1& LanguageId=1 Newmont (2005b) Now & Beyond: Sustainability Reports. Newmont Mining Corporation. Retrieved from http://www.newmont.com/en/social/reporting/ index.asp technologyComment of gold production (CA): 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. UNDERGROUND MINING: Some ore bodies are more economically mined underground. In this case, a tunnel called an adit or a shaft is dug into the earth. Sort tunnels leading from the adit or shaft, called stopes, are dug to access the ore. The surface containing the ore, called a face, is drilled and loaded with explosives. Following blasting, the broken ore is loaded onto electric trucks and taken to the surface. Once mining is completed in a particular stope, it is backfilled with a cement compound. 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. BENEFICIATION: In the Porcupine Mines, gold is recovered using a combination of gravity concentration, milling and cyanidation techniques. The milling process consists of primary crushing, secondary crushing, rod/ball mill grinding, gravity concentration, cyanide leaching, carbon-in-pulp gold recovery, stripping, electrowinning and refining. In the Campbell Mine, the ore from the mine, after crushing and grinding, is processed by gravity separation, flotation, pressure oxidation, cyanidation and carbon-in-pulp process followed by electro-winning and gold refining to doré on site. The Musselwhite Mine uses gravity separation, carbon in pulp, electro¬winning and gold refining to doré on site. REFINING: Wohlwill electrolysis. It is assumed that the gold doré-bars from both mines undergo the treatment of Wohlwill electrolysis. This process uses an electrolyte containing 2.5 mol/l of HCl and 2 mol/l of HAuCl4 acid. Electrolysis is carried out with agitation at 65 – 75 °C. The raw gold is intro-duced as cast anode plates. The cathodes, on which the pure gold is deposited, were for many years made of fine gold of 0.25 mm thickness. These have now largely been replaced by sheet titanium or tantalum cathodes, from which the thick layer of fine gold can be peeled off. In a typical electrolysis cell, gold anodes weighing 12 kg and having dimensions 280×230×12 mm (0.138 m2 surface) are used. Opposite to them are conductively connected cathode plates, arranged by two or three on a support rail. One cell normally contains five or six cathode units and four or five anodes. The maximum cell voltage [V] is 1.5 V and the maximum anodic current density [A] 1500 A/m2. The South African Rand refinery gives a specific gold production rate of 0.2 kg per hour Wohlwill electrolysis. Assuming a current efficiency of 95% the energy consumption is [V] x [A] / 0.2 [kg/h] = 1.63 kWh per kg gold refined. No emissions are assumed because of the purity and the high value of the material processed. The resulting sludge contains the PGM present in the electric scrap and is sold for further processing. WATER EMISSIONS: Effluents are discharged into the ocean. REFERENCES: Newmont (2004) How gold is mined. Newmont. Retrieved from http://www.newmont.com/en/gold/howmined/index.asp Renner H., Schlamp G., Hollmann D., Lüschow H. M., Rothaut J., Knödler A., Hecht C., Schlott M., Drieselmann R., Peter C. and Schiele R. (2002) Gold, Gold Alloys, and Gold Compounds. In: Ullmann's Encyclopedia of Industrial Chemistry. Online version, posting date: September 15, 2000 Edition. Wiley-Interscience, Online-Version under: http://dx.doi.org/10.1002/14356007.a12_ 499. Auerswald D. A. and Radcliffe P. H. (2005) Process technology development at Rand Refinery. In: Minerals Engineering, 18(8), pp. 748-753, Online-Version under: http://dx.doi.org/10.1016/j.mineng.2005.03.011. technologyComment of gold production (AU): 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. UNDERGROUND MINING: Some ore bodies are more economically mined underground. In this case, a tunnel called an adit or a shaft is dug into the earth. Sort tunnels leading from the adit or shaft, called stopes, are dug to access the ore. The surface containing the ore, called a face, is drilled and loaded with explosives. Following blasting, the broken ore is loaded onto electric trucks and taken to the surface. Once mining is completed in a particular stope, it is backfilled with a cement compound. 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. 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. REFINING: Wohlwill electrolysis. It is assumed that the gold doré-bars from both mines undergo the treatment of Wohlwill electrolysis. This process uses an electrolyte containing 2.5 mol/l of HCl and 2 mol/l of HAuCl4 acid. Electrolysis is carried out with agitation at 65 – 75 °C. The raw gold is intro-duced as cast anode plates. The cathodes, on which the pure gold is deposited, were for many years made of fine gold of 0.25 mm thickness. These have now largely been replaced by sheet titanium or tantalum cathodes, from which the thick layer of fine gold can be peeled off. In a typical electrolysis cell, gold anodes weighing 12 kg and having dimensions 280×230×12 mm (0.138 m2 surface) are used. Opposite to them are conductively connected cathode plates, arranged by two or three on a support rail. One cell normally contains five or six cathode units and four or five anodes. The maximum cell voltage [V] is 1.5 V and the maximum anodic current density [A] 1500 A/m2. The South African Rand refinery gives a specific gold production rate of 0.2 kg per hour Wohlwill electrolysis. Assuming a current efficiency of 95% the energy consumption is [V] x [A] / 0.2 [kg/h] = 1.63 kWh per kg gold refined. No emissions are assumed because of the purity and the high value of the material processed. The resulting sludge contains the PGM present in the electric scrap and is sold for further processing. WATER EMISSIONS: Water effluents are discharged into rivers. REFERENCES: Newmont (2004) How gold is mined. Newmont. Retrieved from http://www.newmont.com/en/gold/howmined/index.asp Renner H., Schlamp G., Hollmann D., Lüschow H. M., Rothaut J., Knödler A., Hecht C., Schlott M., Drieselmann R., Peter C. and Schiele R. (2002) Gold, Gold Alloys, and Gold Compounds. In: Ullmann's Encyclopedia of Industrial Chemistry. Online version, posting date: September 15, 2000 Edition. Wiley-Interscience, Online-Version under: http://dx.doi.org/10.1002/14356007.a12_ 499. Auerswald D. A. and Radcliffe P. H. (2005) Process technology development at Rand Refinery. In: Minerals Engineering, 18(8), pp. 748-753, Online-Version under: http://dx.doi.org/10.1016/j.mineng.2005.03.011. technologyComment of gold production (TZ): The mining of ore from open pit and underground mines is considered. technologyComment of gold refinery operation (ZA): REFINING: The refinery, which provides a same day refining service, employs the widely used Miller Chlorination Process to upgrade the gold bullion it receives from mines to at least 99.50% fine gold, the minimum standard required for gold sold on the world bullion markets. It also employs the world’s leading silver refining technology. To further refine gold and silver to 99.99% the cost-effective once-through Wohlwill electrolytic refining process is used. MILLER CHLORINATION PROCESS: This is a pyrometallurgical process whereby gold dore is heated in furnace crucibles. The process is able to separate gold from impurities by using chlorine gas which is added to the crucibles once the gold is molten. Chlorine gas does not react with gold but will combine with silver and base metals to form chlorides. Once the chlorides have formed they float to the surface as slag or escape as volatile gases. The surface melt and the fumes containing the impurities are collected and further refined to extract the gold and silver. This process can take up to 90 minutes produces gold which is at least 99.5% pure with silver being the main remaining component. This gold can be cast into bars as 99.5% gold purity meets the minimum London Good Delivery. However some customers such as jewellers and other industrial end users require gold that is almost 100% pure, so further refining is necessary. In this case, gold using the Miller process is cast into anodes which are then sent to an electrolytic plant. The final product is 99.99% pure gold sponge that can then be melted to produce various end products suited to the needs of the customer. WOHLWILL PROCESS - The electrolytic method of gold refining was first developed by Dr. Emil Wohlwill of Norddeutsche Affinerie in Hamburg in 1874. Dr. Wohlwill’s process is based on the solubility of gold but the insolubility of silver in an electrolyte solution of gold chloride (AuCl3) in hydrochloric acid. Figure below provide the overview of the refining process (source Rand Refinery Brochure) imageUrlTagReplace7f46a8e2-2df0-4cf4-99a8-2878640be562 Emissions includes also HCl to air: 7.48e-03 Calculated from rand refinery scrubber and baghouse emmission values Metal concentrators, Emmision report 2016 http://www.environmentalconsultants.co.za/wp-content/uploads/2016/11/Appendix-D1.pdf technologyComment of gold refinery operation (RoW): REFINING: The refinery, which provides a same day refining service, employs the widely used Miller Chlorination Process to upgrade the gold bullion it receives from mines to at least 99.50% fine gold, the minimum standard required for gold sold on the world bullion markets. It also employs the world’s leading silver refining technology. To further refine gold and silver to 99.99% the cost-effective once-through Wohlwill electrolytic refining process is used. MILLER CHLORINATION PROCESS: This is a pyrometallurgical process whereby gold dore is heated in furnace crucibles. The process is able to separate gold from impurities by using chlorine gas which is added to the crucibles once the gold is molten. Chlorine gas does not react with gold but will combine with silver and base metals to form chlorides. Once the chlorides have formed they float to the surface as slag or escape as volatile gases. The surface melt and the fumes containing the impurities are collected and further refined to extract the gold and silver. This process can take up to 90 minutes produces gold which is at least 99.5% pure with silver being the main remaining component. This gold can be cast into bars as 99.5% gold purity meets the minimum London Good Delivery. However some customers such as jewellers and other industrial end users require gold that is almost 100% pure, so further refining is necessary. In this case, gold using the Miller process is cast into anodes which are then sent to an electrolytic plant. The final product is 99.99% pure gold sponge that can then be melted to produce various end products suited to the needs of the customer. WOHLWILL PROCESS - The electrolytic method of gold refining was first developed by Dr. Emil Wohlwill of Norddeutsche Affinerie in Hamburg in 1874. Dr. Wohlwill’s process is based on the solubility of gold but the insolubility of silver in an electrolyte solution of gold chloride (AuCl3) in hydrochloric acid. Figure below provide the overview of the refining process (source Rand Refinery Brochure) imageUrlTagReplace7f46a8e2-2df0-4cf4-99a8-2878640be562 Emissions includes also HCl to air: 7.48e-03 Calculated from rand refinery scrubber and baghouse emmission values Metal concentrators, Emmision report 2016 http://www.environmentalconsultants.co.za/wp-content/uploads/2016/11/Appendix-D1.pdf 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 platinum group metal, extraction and refinery operations (ZA): The ores from the different ore bodies are processed in concentrators where a PGM concentrate is produced with a tailing by product. The PGM base metal concentrate product from the different concentrators processing the different ores are blended during the smelting phase to balance the sulphur content in the final matte product. Smelter operators also carry out toll smelting from third part concentrators. The smelter product is send to the Base metal refinery where the PGMs are separated from the Base Metals. Precious metal refinery is carried out on PGM concentrate from the Base metal refinery to split the PGMs into individual metal products. Water analyses measurements for Anglo Platinum obtained from literature (Slatter et.al, 2009). Mudd, G., 2010. Platinum group metals: a unique case study in the sustainability of mineral resources, in: The 4th International Platinum Conference, Platinum in Transition “Boom or Bust.” Water share between MC and EC from Mudd (2010). Mudd, G., 2010. Platinum group metals: a unique case study in the sustainability of mineral resources, in: The 4th International Platinum Conference, Platinum in Transition “Boom or Bust.” 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 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
Four free-air CO2 enrichment (FACE) experiments were conducted on wheat (Triticum aestivum L. cv. Yecora Rojo) at Maricopa, Arizona, U.S.A. from December, 1992 through May, 1997. The first two were conducted at ample and limited (50% of ample) supplies of water, and second two at ample (350 kg N ha-1) and limited (70 and 15 kg N ha-1) supplies of fertilizer nitrogen. More than 50 scientists participated, and they collected a large and varied set of data on plant, soil, and microclimatic responses to the elevated CO2 and its interactions with the water and N treatments. The dataset has been popular with wheat growth modelers who have utilized the growth, yield, and other data to validate their models, which get used to predict likely future wheat productivity with projected global change. The dataset assembled herein contains many of these data, including management, soils, weather, physiology, phenology, biomass growth, leaf area, yield, quality, canopy temperatures, energy balance, soil moisture, nitrogen assimilation, and other data. Quelle: Verlagsinformation
Die Siemens Energy Global GmbH & Co. KG hat mit Datum vom 19.08.2022 bei der Bezirksregierung Düsseldorf als zuständiger Genehmigungsbehörde einen Antrag auf Erteilung einer Genehmigung nach §§ 4, 6 BImSchG zur Errichtung und zum Betrieb von zwei Dampfkesselanlagen gestellt. Die zwei Dampfkesselanlagen mit einer Feuerungswärmeleistung von je 45,2 MW sollen für die Bereitstellung von Dampf für die Tests von Dampfturbinen maximal 350 Stunden im Jahr betrieben werden und auf dem Grundstück Wolfgang-Reuter-Platz 4 in 47053 Duisburg-Hochfeld, Gemarkung Duisburg, Flur 308, Flurstück 79, 123 errichtet werden. Gegenstand des Antrags sind im Wesentlichen die Errichtung und der Betrieb von: • zwei gasgefeuerten Dampfkesselanlagen mit einer Feuerungswärmeleistung von je 45,2 MW, • einem Speisewasserbehälter, • einer Wasseraufbereitungsanlage, bestehend aus Filter, Enthärtungsanlage, Umkehrosmoseanlage sowie Mischbettionenaustauscher und Entgaser, • einem gemeinsamen Schornstein für die beiden Dampfkesselanlagen, • den zugehörigen Rohrleitungen, Dosiereinrichtungen, Pumpen etc.
Ein Priorisierungsrahmenwerk wurde entwickelt, um die Auswahl derjenigen PMT/vPvM Stoffe zu unterstützen, die sofortige Maßnahmen durch REACH-Registranten, Regulierungsbehörden, Forschern und dem Wassersektor erfordern, um die Trinkwasserressourcen vor einer Kontamination zu schützen. Das entwickelte Rahmenwerk ist das Ergebnis von Stakeholder-Befragungen, Monitoringkampagnen, Laboruntersuchungen, Literaturrecherchen und einem Stakeholder-Workshop. Das Rahmenwerk für die Priorisierung von PMT/vPvM-Stoffen basiert auf den folgenden fünf Priorisierungskategorien: I) die PMT/vPvM-Gefahrenbewertung; II) die REACH-Emissionswahrscheinlichkeit; III) die Analytik und Monitoringlücken; IV) die Wasseraufbereitungslücke und v) das Expositionsniveau. Zur Umsetzung dieses Priorisierungsrahmenwerks wurden 176 Stoffe auf der Grundlage mehrerer Überlegungen ausgewählt. Zu den Auswahlkriterien gehörten, ob sie die PMT/vPvM-Kriterien erfüllen oder nicht, Datenlücken in Bezug auf die PMT/vPvM-Bewertung, ob sie eine Perfluoralkyl-Substruktur oder Triazin-Substruktur enthalten, der Verdacht, in deutschen Trinkwasserressourcen vorhanden zu sein, und aktuelle Kenntnisse zu Analytikmethoden. Die PMT/vPvM-Gefahrenbewertung wurde für alle 176 Stoffe durchgeführt, und es wurde festgestellt, dass 99 die PMT/vPvM-Kriterien erfüllten. Die REACH Emissionswahrscheinlichkeit konnte für 152 der 176 Stoffe abgeleitet werden, und es wurde festgestellt, dass 133 von ihnen entweder eine "hohe" (84 Stoffe) oder "sehr hohe" (49 Stoffe) REACH-Emissionswahrscheinlichkeit aufwiesen. Die Analyse- und Monitoringlücken und die Wasseraufbereitungslücke wurden für 150 der Stoffe durch eine Umfrage bei Analyselaboren und Wasseraufbereitungsanlagen in ganz Deutschland sowie durch eigene experimentelle Arbeiten untersucht. Bei dieser Untersuchung wurde festgestellt, dass 26 Stoffe eine geringe bis erhebliche Analytiklücke und 58 Stoffe eine erhebliche Monitoringlücke aufweisen. Es gab erhebliche Wasseraufbereitungslücken für die untersuchten Substanzen, da 78 weder durch Aktivkohlefilter noch durch Ozonung entfernt werden können, 22 können nur durch Ozonung und 31 nur durch Aktivkohlefilter entfernt werden. Die Expositionswerte wurden durch eine Monitoringstudie von 78 der 176 Substanzen in 13 Trinkwassereinzugsgebieten zu zwei verschiedenen Zeitpunkten untersucht. Dies wurde durch eine Literaturrecherche ergänzt, in der Monitoringdaten für 12 Stoffe gefunden wurden, die nicht in die Monitoringkampagne aufgenommen wurden. Davon waren 10 der Substanzen allgegenwärtig in hohen Konzentrationen, 28 allgegenwärtig in niedrigen Konzentrationen und 36, die in lokalen Regionen entweder in hohen oder niedrigen Konzentrationen überwacht wurden. Aus der Bewertung dieser fünf Priorisierungskategorien ergeben sich durch das Priorisierungsrahmenwerk 43 PMT/vPvM-Stoffe mit höchster Priorität, 23 Stoffe mit hoher Priorität und 33 Stoffe mit mittlerer Priorität für Folgemaßnahmen. Das hier vorgestellte Priorisierungsrahmenwerk kann als Frühwarnsystem dienen, um eine unmittelbare Bedrohungen oder Besorgnis durch andere als in dieser Studie berücksichtigen PMT/vPvM oder potenzielle PMT/vPvM-Stoffe zu identifizieren. Quelle: Forschungsberichte
Die MM Neuss GmbH hat mit Datum vom 20.12.2022, zuletzt ergänzt am 27.04.2023, einen Antrag auf Genehmigung nach § 16 BImSchG zur wesentlichen Änderung der Anlage zur Herstellung von Pappe und Karton durch Errichtung und Betrieb einer Wasseraufbereitungsanlage für die Erzeugung von Prozesswasser, Betriebswasser und vollentsalztem Wasser (WAB) auf dem Betriebsgelände Düsseldorfer Str. 182 - 184 in 41460 Neuss gestellt. Der Antragsgegenstand umfasst im Wesentlichen die Errichtung und den Betrieb einer Wasseraufbereitungsanlage für die Erzeugung von Prozesswasser, Betriebswasser und vollentsalztem Wasser als Ersatz für die am Standort betriebene Wasseraufbereitungsanlage.
Die Stadtwerke Stuttgart GmbH plant Am Mittelkai 25 in 70327 Stuttgart die Errich-tung und den Betrieb einer Anlage zur Herstellung von grünem Wasserstoff (sog. Green Hydrogen Hub Stuttgart (GHHS)) auf dem Flurstück-Nr. 1500/16, Gemarkung Stuttgart. Die geplante Anlage zur Herstellung von Wasserstoff umfasst den Dauerbe-trieb von vier baugleichen PEM-Elektrolyseuren mit einer elektrischen Leistung von jeweils bis zu 2,5 MWel, also insgesamt 10 MWel und der dazugehörigen Anlagenteile zur Produktion von bis zu 4.320 kg Wasserstoff pro Tag. Anstelle des dritten PEM-Elektrolyseurs soll für eine Dauer von maximal zwei Jahren ein alkalischer For-schungselektrolyseurs (AEL) mit einer elektrischen Leistung von 1 MW zur Produktion von bis zu 432 kg Wasserstoff pro Tag betrieben werden. An diesem Elektrolyseur wird das Zentrum für Sonnenenergie- und Wasserstoffforschung (ZSW) Forschungen durchführen, Betreiber bleibt jedoch die Stadtwerke Stuttgart GmbH. Die Anlage zur Herstellung von Wasserstoff soll im Wesentlichen aus folgenden Anla-genteilen bestehen: • Transformatorenstation zur Umspannung von 10 kV auf 0,4 bzw. 0,515 kV • Batteriespeicher mit einer Speicherkapazität von 2 MWh • Vier Elektrolyse-Containern inklusive den PEM-Elektrolyseuren 1 bis 4 (alternativ für zwei Jahre ein AEL-Elektrolyseur), Wasseraufbereitungsanlage, Wasserstoff-reinigungsanlage und Druckluftversorgung • Einem BoP-Container (Balance of Plant) inklusive Gleichrichtern und Kühlkreis-laufanbindung für den AEL-Elektrolyseur • Vier E-Containern inklusive Mittelspannungstransformatoren, Mittelspannungs-schaltanlage und Gleichrichtern • den ND-Wasserstoffpufferspeichern 1 und 2 mit einer Speicherkapazität von jeweils 2 kg Wasserstoff bei einem Betriebsdruck von bis zu 3,1 bar(a) • den ND-Wasserstoffspeichern 1 und 2 mit einer Speicherkapazität von jeweils 218,3 kg Wasserstoff bei einem Betriebsdruck von bis zu 8,1 bar(a) • einem HD-Wasserstoffspeicher mit einer Speicherkapazität von bis zu 1.559 kg bei einem Betriebsdruck von bis zu 50,1 bar(a) • den Wasserstoff-Kompressoren 1 und 2 mit einer Leistung von jeweils 250 kW zur Verdichtung von Wasserstoff auf bis zu 50,1 bar(a) • einem Container inklusive Wasserstoffverteilstation, Qualitätsmessung, Anla-gensteuerung und Anschluss für an die Wasserstoffpipeline • den LKW-Abfüllpaneelen 1 bis 3 zur Abfüllung von jeweils bis zu 360 kg Was-serstoff pro Stunde • einem Betriebsgebäude • einer Luftzerlegungsanlage mit einer Leistung von 10 Nm³ Stickstoff pro Stunde • einer Wärmeübergabestation • einem Pipelineanschluss • Leerkanal für ggf. spätere Sauerstoffnutzung Der erzeugte Wasserstoff soll entweder über die Pipeline direkt abgegeben oder in Wasserstoff-Trailer verladen werden. Ferner soll auch die Möglichkeit bestehen, die ND-Wasserstoffspeicher mit Wasserstoff aus den Wasserstoff-Trailern zu befüllen. Die Abwärme aus den Elektrolyseanlagen soll mittels Wärmetauschern an eine zent-rale Wärmeübergabestation übergeben und in ein Wärmenetz eingespeist werden. Der alkalische Forschungselektrolyseur soll in dieses Wärmenetz nicht eingebunden werden. Eine Lagerung (Aufenthalt von mehr als 24 Stunden bzw. am Wochenende mehr als 72 Stunden) der befüllten Wasserstoff-Trailer ist nicht geplant. Für das Vorhaben beantragte die Stadtwerke Stuttgart GmbH am 01.02.2024 die Er-teilung einer immissionsschutzrechtlichen Genehmigung gemäß § 4 BImSchG beim Regierungspräsidium Stuttgart.
Die WHW Langenfeld GmbH & Co. KG hat mit Datum vom 16.03.2023, zuletzt ergänzt am 13.10.2023, einen Antrag auf Genehmigung nach § 16 BImSchG zur wesentlichen Änderung des Oberflächenbehandlungsanlage (72,2 m³) u. a.durch Errichtung neuer Lösestationen auf dem Betriebsgelände Friedrich-Krupp-Str. 12 in 40764 Langenfeld gestellt. Der Antragsgegenstand umfasst im Wesentlichen die folgenden Maßnahmen: • die Errichtung einer Online-Analytik zur Steuerung der Becken, den Umbau bestehender Lösestationen und die Errichtung sowie Demontage weiterer Behälter in der Anlage 40, • die Demontage eines Sammelbehälters für Abwasser in der Anlage 41, • die zusätzliche Aufstellung zweier Bereitstellungs-/Dosierbehälter in der Anlage 42 • die Errichtung eines Blocklagers anstatt eines Regallagers im Bereich der Wasseraufbereitungsanlage und Umbenennung von Chemikaliencontainern sowie • die Einführung einer weiteren Lagervariante im Chemikaliencontainer 2.
Perfluoroalkyl substances (PFAS) persistence in the environment leads to their presence in drinking water, that is of high concern due to their potential human health risk. Adsorption onto activated carbon (AC) has been identified as an effective technique to remove PFAS. Adsorption isotherms and breakthrough curves, determined by rapid small-scale column tests (RSSCTs), were studied for eight PFAS and four granular ACs, characterized by different origins, porosities and numbers of reactivation cycles. Both batch and RSSCT results highlighted the strong interaction of AC and PFAS characteristics in adsorption capacity. The most important factor affecting AC performance is the surface charge: a positively-charged AC showed higher adsorption capacities with greater Freundlich constants (KF) and later 50% breakthroughs compared to the AC with neutral surface. Among the positively-charged ACs, a microporous AC demonstrated higher adsorption capacities for hydrophilic and marginally hydrophobic PFAS, while the mesoporous AC performed better for more hydrophobic PFAS, possibly due to lower pore blockage by organic matter. These results were confirmed at full-scale through a one-year monitoring campaign, in which samples were collected at the inlets and outlets of GAC systems in 17 drinking water treatment plants spread in a wide urban area, where the four analyzed ACs are used. © 2021 Elsevier B.V.
The cyanotoxin cylindrospermopsin was discovered during a drinking water-related outbreak of human poisoning in 1979. Knowledge about the degradation of cylindrospermopsin in waterbodies is limited. So far, only few cylindrospermopsin-removing bacteria have been described. Manganese-oxidizing bacteria remove a variety of organic compounds. However, this has not been assessed for cyanotoxins yet. We investigated cylindrospermopsin removal by manganese-oxidizing bacteria, isolated from natural and technical systems. Cylindrospermopsin removal was evaluated under different conditions. We analysed the correlation between the amount of oxidized manganese and the cylindrospermopsin removal, as well as the removal of cylindrospermopsin by sterile biogenic oxides. Removal rates in the range of 0.4-37.0(my)L-1 day-1 were observed. When MnCO3 was in the media Pseudomonas sp. OF001 removed round about 100% of cylindrospermopsin in 3 days, Comamonadaceae bacterium A210 removed round about 100% within 14 days, and Ideonella sp. A288 and A226 removed 65% and 80% within 28 days, respectively. In the absence of Mn2+, strain A288 did not remove cylindrospermopsin, while the other strains removed 5-16%. The amount of manganese oxidized by the strains during the experiment did not correlate with the amount of cylindrospermopsin removed. However, the mere oxidation of Mn2+ was indispensable for cylindrospermopsin removal. Cylindrospermopsin removal ranging from 0 to 24% by sterile biogenic oxides was observed. Considering the efficient removal of cylindrospermopsin by the tested strains, manganese-oxidizing bacteria might play an important role in cylindrospermopsin removal in the environment. Besides, manganese-oxidizing bacteria could be promising candidates for biotechnological applications for cylindrospermopsin removal in water treatment plants. © 2019 Elsevier Ltd.
Für die Verbandsgemeinde Bad Ems - Nassau, vertreten durch die Verbandsgemeindewerke Bad Ems - Nassau, Koppelheck 24, 56377 Nassau, wurde mit Datum vom 20.01.2020 die wasserrecht-liche Erlaubnis zur Grundwasserentnahme von 700.000 m³/a erteilt zum Zweck der öffentlichen Wasserversorgung für die Ortslagen Fachbach, Fachbach-Oberau, Nievern, Miellen, Zentrum und Hochzone von Bad Ems, Kemmenau, Arzbach und Dausenau (über die Wasseraufbereitungsanlage „Fachbach“, WWK-Nr.: 323 215 361). Für die Benutzung ist gem. § 7 Abs. 1 UVPG i. V. m. Anlage 1, Nr. 13.3.2 UVPG, bei Vorhaben mit einer Größe oder Leistung ab 100.000 m³ eine allgemeine Vorprüfung des Einzelfalls zur Feststel-lung der UVP-Pflicht in Bezug auf die Schutzkriterien gem. Anlage 3 UVPG durchzuführen. Diese allgemeine Vorprüfung hat ergeben, dass das Vorhaben keine erheblichen nachteiligen Um-weltauswirkungen hat und somit in der Folge die Durchführung einer Umweltverträglichkeitsprüfung ebenfalls nicht erforderlich ist. Bereits im vorherigen Erlaubnisverfahren von 2015 konnten keine nachteiligen Auswirkungen ermit-telt werden, so dass im aktuellen Erlaubnisverfahren keine Verschlechterung zu erwarten ist. Dies wurde gem. § 5 Abs. 2 UVGP durch die Bekanntmachung im Mitteilungsblatt der Verbands-gemeinde Bad Ems - Nassau in der Ausgabe 49/2019 vom 05.12.2019 veröffentlicht. Parallel dazu erfolgt noch eine Veröffentlichung im zentralen UVP-Portal Rheinland-Pfalz (https://www.uvp-verbund.de/rp).
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