Dieser Datensatz enthält Bereiche, Unterbereiche und Zonen der Naturschutzgebiete im Bereich der deutschen ausschließlichen Wirtschaftszone und des Festlandsockels gemäß den Verordnungen vom 28.09.2017 (Bundesgesetzblatt Jahrgang 2017 Teil Nr. 63).
Downloaddienst für die in den sechs Naturschutzgebietsverordnungen enthaltenen Geoinformationen. Die Verordnungen der Naturschutzgebiete (NSG-VO) in der deutschen ausschließlichen Wirtschaftszone (AWZ) von Nord- und Ostsee wurden am 28.09.2017 im Bundesgesetzblatt Jahrgang 2017 Teil Nr. 63 veröffentlicht und enthalten Geoinformationen zu Außengrenzen, zu Unterteilungen, zu Eckpunkten mit ihren Koordinaten und zu Maßnahmen. Die Maßnahmen regulieren Freizeitfischerei, Aquakultur, das Ausbringen von Baggergut sowie das Ausbringen gebietsfremder Tier- und Pflanzenarten in den NSG.
Darstellungsdienst für die in den sechs Naturschutzgebietsverordnungen enthaltenen Geoinformationen. Die Verordnungen der Naturschutzgebiete (NSG-VO) in der deutschen ausschließlichen Wirtschaftszone (AWZ) von Nord- und Ostsee wurden am 28.09.2017 im Bundesgesetzblatt Jahrgang 2017 Teil Nr. 63 veröffentlicht und enthalten Geoinformationen zu Außengrenzen, zu Unterteilungen, zu Eckpunkten mit ihren Koordinaten und zu Maßnahmen. Die Maßnahmen regulieren Freizeitfischerei, Aquakultur, das Ausbringen von Baggergut sowie das Ausbringen gebietsfremder Tier- und Pflanzenarten in den NSG.
Plassmann, Merle M.; Fischer, Stellan; Benskin, Jonathan P. Environ. Sci. Technol. Lett. 5 (2018), 6, 335-340 Human biomonitoring (HBM) programs monitor exposure to a limited number of prioritized chemicals resulting in some important substances being overlooked. Nontarget analysis shows promise for capturing novel substances, yet the large quantity of data produced by these methods remains challenging to interrogate. Here, we apply a prioritization strategy for temporal nontarget HBM data, which shortlists features with increasing time trends, possibly representing substances which are bioaccumulating or to which humans are increasingly exposed. Human whole blood sampled in Germany between 1983 and 2015 was extracted using a modified QuEChERS method and analyzed by UHPLC-Oribtrap-mass spectrometry. Following alignment, peak detection, grouping, and gap filling, up to 14,460 features were obtained. This number was reduced to ≤716 using time trend ratios and Spearman’s rank correlation coefficients to identify features which increased over the 32-year time series. Increasing features were investigated further using the KemI market list database (which prioritizes based on human hazard and/or exposure potential) as well as data-dependent product ion scans, followed by MetFrag and mzCloud database searches. Finally, seven prioritized substances, including one pharmaceutical, two pesticides, and four performance chemicals, were confirmed using standards, demonstrating the potential of time trend screening as a prioritization strategy for nontarget HBM data. doi:10.1021/acs.estlett.8b00196 Siehe auch: Biomonitoring of new contaminants: Sub-Project 2 – Screening of target and non-target contaminants in human blood and urine
Blei tritt hauptsächlich in den Oxidationsstufen +2 und +4 auf. In der Wasserphase kommt es meist in der Stufe +2 vor. Die Menge des löslichen Bleis hängt vom pH-Wert, dem Redoxpotential sowie der Grundmineralisierung des Wassers ab. Der Transport erfolgt überwiegend in kolloidgebundener Form, so dass Ablagerungen in Sedimenten weit verbreitet sind. Gediegenes Blei ist in der Natur relativ selten. Bleierze können unterschiedliche Mengen an Silber (Ag), Zink (Zn), Kupfer (Cu), Arsen (As), Antimon (Sb) und auch Wismut (Bi) enthalten. Blei kann als zweiwertiges Ion Calcium in Silikaten und Phosphaten substituieren. Der technische Einsatz von Blei ist auch heute noch sehr vielfältig. Sowohl metallisches Blei als auch seine Verbindungen sind toxisch, wobei die Ausscheidung aus dem lebenden Organismus meist gering ist (Einlagerung und Anreicherung in den Knochen und Haaren). Der Schwellenwert nach GrwV beträgt für Blei 10 µg/l. Weitere Informationen zum Thema finden Sie hier .
technologyComment of chlor-alkali electrolysis, diaphragm cell (RER): In the diaphragm process, all reactions take place in only one cell. A diaphragm is used to separate the feed brine (anolyte) and the chlorine formed at the anode from the sodium hydroxide containing solution (catholyte) and the hydrogen formed at the cathode. Without the diaphragm being present during electrolysis, chlorine and hydrogen would form an explosive mixture and sodium hydroxide and chlorine would react to form sodium hypochlorite (NaOCl). Diaphragms used to be made from asbestos but up-todate technology allows for asbestos-free polymer-based diaphragms. Purified brine is fed to the anode compartment and percolates through the diaphragm into the cathode compartment. The percolation rate is controlled by a difference in liquid level between both compartments. At the anodes (metal oxide coated titanium), chlorine gas is formed which is collected and directed to further processing. Cathodes, where water decomposition takes place, are made of activated carbon steel. Catholyte leaving the cell, also called cell liquor, is a mixture of 10-12 wt.-% sodium hydroxide and 15-17 wt.-% sodium chloride in water. This solution is usually evaporated to 50 wt.-% NaOH. In this process, simultaneously most of the salt is removed by precipitation to a final residual of 1 wt.-%. The resulting salt is typically recirculated to brine preparation. The advantage of diaphragm cells is that the quality requirements for the brine and the electrical energy consumption are low. Disadvantageous are the high amount of thermal energy necessary for sodium hydroxide concentration and the comparably low quality of the produced sodium hydroxide and chlorine. References: Euro Chlor (2013) An Eco-profile and Environmental Product Declaration of the European Chlor-Alkali Industry, Chlorine (The chlor-alkali process). technologyComment of chlor-alkali electrolysis, membrane cell (RER): In the membrane cell process, the anode and cathode compartments are separated by a perfluoropolymer cation-exchange membrane that selectively transmits sodium ions but suppresses the migration of hydroxyl ions (OH-) from the catholyte into the anolyte. Saturated brine flows through the anode compartment, where chlorine gas is produced at the anode. The electric field in the electrolysis cell causes hydrated sodium ions to migrate through the membrane into the cathode compartment. The cathode compartment is fed with diluted sodium hydroxide solution. Water is electrolysed at the cathode releasing gaseous hydrogen and hydroxyl ions, which combine with the sodium ions and thus increase the concentration of sodium hydroxide in the catholyte. Typically, the outlet concentration of sodium hydroxide is around 32 wt.-%. A part of the product stream is diluted with demineralised water to about 30 wt.-% and used as catholyte inlet. In some units, a more diluted 23 wt.-% NaOH solution is produced. In these cases, the inlet concentration is adjusted to 20-21 wt.-%. Usually the NaOH solution is evaporated to the marketable concentration of 50 wt.-% using steam. Depleted brine leaving the anode compartment is saturated with chlorine and is therefore sent to a dechlorination unit to recover the dissolved chlorine before it is resaturated with salt for recirculation. The advantages of the membrane cell technique are the very high purity of the sodium hydroxide solution produced and the comparably low energy demand. Disadvantages comprise the high requirements on brine purity, the need for sodium hydroxide evaporation to increase concentration, and the comparably high oxygen content in the produced chlorine. In general, multiple cell elements are combined into a single unit, called electrolyser, of whom the design can be either monopolar or bipolar. In a monopolar electrolyser, the anodes and cathodes of the cells are connected electrically in parallel, whereas in the bipolar design, they are connected in series. Therefore, monopolar electrolysers require high current and low voltage, whereas bipolar electrolysers require low current and high voltage. Since bipolar systems allow higher current densities inside the cells, investment and operating costs are usually lower than for monopolar systems. References: Euro Chlor (2013) An Eco-profile and Environmental Product Declaration of the European Chlor-Alkali Industry, Chlorine (The chlor-alkali process). technologyComment of chlor-alkali electrolysis, mercury cell (RER): The mercury cell process comprises an electrolysis cell and a decomposer. Purified and saturated brine (25-28 wt.-% NaCl in water) is fed to the electrolysis cell on top of a film of mercury (Hg) flowing down the inclined base of the cell. The base of the cell is connected to the negative pole of a direct current supply forming the cathode of the cell. Anodes consisting of titanium coated with oxides of ruthenium and titanium are placed in the brine without touching the mercury film. At the anodes, chlorine gas is formed which is collected and directed to further processing. Due to a high overpotential of hydrogen at the mercury electrode, no gaseous hydrogen is formed; instead, sodium is produced and dissolved in the mercury as an amalgam (mercury alloy). The liquid amalgam is removed from the electrolytic cell and fed to a decomposer, where it reacts with demineralised water in the presence of a graphite-based catalyst to form sodium hydroxide solution and hydrogen. The sodium-free mercury is recirculated back into the cell. Cooling of hydrogen is essential to remove any water and mercury. The sodium hydroxide solution is very pure, almost free from chloride contamination and has usually a concentration of 50 %. Further treatment comprises cooling and removal of catalyst and mercury traces by centrifuges or filters. Advantages of the mercury cell process are the high quality of chlorine and the high concentration and purity of sodium hydroxide solution produced. The consumption of electric energy for electrolysis is, however, higher than for the other techniques and a high purity of the feed brine is required. Inherently, the use of mercury gives rise to environmental releases of mercury. References: Euro Chlor (2013) An Eco-profile and Environmental Product Declaration of the European Chlor-Alkali Industry, Chlorine (The chlor-alkali process). technologyComment of potassium hydroxide production (RER): Potassium hydroxide is manufactured by the electrolysis of potassium chloride brine in electrolytical cells. Hydrogen and chlorine are withdrawn from the cell. The rest of the reaction mixture contains KOH, water, and unreacted potassium chloride. This reaction mixture is then concentrated in an evaporator. Most of the potassium chloride crystallizes by evaporation, and is recycled. After evaporation, the potassium hydroxide is precipitated. Potassium hydroxide, chlorine and hydrogen are obtained from potassium chloride brine according to the following reaction: 2 KCl + 2 H2O -> 2 KOH + Cl2 + H2 Reference: Jungbluth, N., Chudacoff, M., Dauriat, A., Dinkel, F., Doka, G., Faist Emmenegger, M., Gnansounou, E., Kljun, N., Schleiss, K., Spielmann, M., Stettler, C., Sutter, J. 2007: Life Cycle Inventories of Bioenergy. ecoinvent report No. 17, Swiss Centre for Life Cycle Inventories, Dübendorf, CH. technologyComment of sodium chloride electrolysis (RER): Sodium chloride electrolysis
In der Umgebung von Hochspannungsleitungen treten erhöhte Konzentrationen von Ionen und geladenen Partikeln auf. Dieser Report untersucht den Stand der Wissenschaft zur Quantifizierung dieser Konzentrationen, sowie zu daraus gegebenenfalls resultierenden gesundheitlichen Implikationen. Hohe Konzentrationen sogenannter Korona-Ionen treten vor allem nahe von Gleichspannungsleitungen auf: zahlreiche Messungen bestätigen, dass die Messwerte den laut der Theorie von KAUNE, GILLIS & WEIGEL (1983a) theoretisch zulässigen Maximalwerten durchaus nahekommen können, diese aber praktisch nie überschreiten. Die Ionen können sich im weiteren Verlauf an Partikel anlagern, dieser Vorgang ist jedoch aufgrund der komplexen Einflussfaktoren schwieriger theoretisch quantifizierbar. Auch Messungen der Konzentration geladener Partikel gestalten sich aufwändig und liegen deshalb kam vor bzw. beschränken sich auf kleine geladene Partikel. Eine Abschätzungsmethode zur Ladungsaufnahme durch Partikel wird präsentiert und mit tatsächlichen Messungen verglichen. Hier besteht noch Forschungsbedarf; dies gilt auch für andere Bereiche, in welchem ebenfalls hohe Konzentrationen geladener Partikel beobachtet wurden, besonders im Verkehrsbereich. Die Haupt-Hypothese zu Gesundheitsgefahren besteht darin, dass geladene Partikel mit höherer Wahrscheinlichkeit in Lunge und Atemtrakt deponiert werden als ungeladene Partikel derselben Größe. Dieser Report konzentriert sich vor allem auf die experimentellen Depositionsstudien von MELANDRI et al. (1983) und COHEN et al. (1995), und kontrastiert die Ergebnisse mit den Erwartungen des ICRP-Modells zur Deposition neutraler Partikel. Trotz einiger Unsicherheiten kann eigeschätzt werden, dass die Partikelbeladungen, welche im Umfeld von Hochspannungsleitungen entstehen, nur zu einer praktisch vernachlässigbaren Erhöhung der Depositionswahrscheinlichkeit führen. Dieser Report bestätigt damit im Wesentlichen die Ergebnisse entsprechender vorhergehender Reviews (NRPB 2004).
Die lokalisierte Mikrobestrahlung von Zellen oder sub-zellulären Strukturen ermöglicht die Bearbeitung einer Reihe von strahlenbiologisch wichtigen Fragen. Aufgrund der aufwändigen Technologie sind jedoch bislang weltweit nur etwa 10 Mikrobestrahlungseinrichtungen, die ionisierende Strahlung nutzen, routinemäßig für biologische Experimente im Einsatz (Gerardi 2006). Viele Experimente zur Schadenserkennung, Signalweitergabe und Rekrutierung von Proteinen nach Induktion von DNA-Doppelstrangbrüchen (DSB) wurden mit Hilfe eines Ersatzsystems gewonnen, nämlich Lasermikrobestrahlung, meist unter Verwendung von UVA-Lasern (Lukas et al. 2005). Da das Spektrum der laserinduzierten Schäden nicht gut charakterisiert ist, stellt sich die Frage, inwieweit die mit den Lasersystemen erzielten Ergebnisse auf ionisierende Bestrahlung übertragbar sind. Ziel des Forschungsvorhabens war der systematische Vergleich der Rekrutierung von DSB-Reparaturproteinen und Signalfaktoren nach Ionenmikrobestrahlung mit unterschiedlichen Ionen und nach UVA-Laserbestrahlung. Verglichen werden sollten die Kinetik der Bildung und die Persistenz der Foci, sowie ihre Anzahl und Anordnung. Dies soll klären, inwieweit die mit den verschiedenen Systemen erzielten Daten in der Literatur vergleichbar sind und die Grundlagen für das Verständnis eventuell auftretender Unterschiede legen.
technologyComment of chlor-alkali electrolysis, diaphragm cell (RER, RoW): In the diaphragm process, all reactions take place in only one cell. A diaphragm is used to separate the feed brine (anolyte) and the chlorine formed at the anode from the sodium hydroxide containing solution (catholyte) and the hydrogen formed at the cathode. Without the diaphragm being present during electrolysis, chlorine and hydrogen would form an explosive mixture and sodium hydroxide and chlorine would react to form sodium hypochlorite (NaOCl). Diaphragms used to be made from asbestos but up-todate technology allows for asbestos-free polymer-based diaphragms. Purified brine is fed to the anode compartment and percolates through the diaphragm into the cathode compartment. The percolation rate is controlled by a difference in liquid level between both compartments. At the anodes (metal oxide coated titanium), chlorine gas is formed which is collected and directed to further processing. Cathodes, where water decomposition takes place, are made of activated carbon steel. Catholyte leaving the cell, also called cell liquor, is a mixture of 10-12 wt.-% sodium hydroxide and 15-17 wt.-% sodium chloride in water. This solution is usually evaporated to 50 wt.-% NaOH. In this process, simultaneously most of the salt is removed by precipitation to a final residual of 1 wt.-%. The resulting salt is typically recirculated to brine preparation. The advantage of diaphragm cells is that the quality requirements for the brine and the electrical energy consumption are low. Disadvantageous are the high amount of thermal energy necessary for sodium hydroxide concentration and the comparably low quality of the produced sodium hydroxide and chlorine. References: Euro Chlor (2013) An Eco-profile and Environmental Product Declaration of the European Chlor-Alkali Industry, Chlorine (The chlor-alkali process). technologyComment of chlor-alkali electrolysis, membrane cell (CA-QC, RER, RoW): In the membrane cell process, the anode and cathode compartments are separated by a perfluoropolymer cation-exchange membrane that selectively transmits sodium ions but suppresses the migration of hydroxyl ions (OH-) from the catholyte into the anolyte. Saturated brine flows through the anode compartment, where chlorine gas is produced at the anode. The electric field in the electrolysis cell causes hydrated sodium ions to migrate through the membrane into the cathode compartment. The cathode compartment is fed with diluted sodium hydroxide solution. Water is electrolysed at the cathode releasing gaseous hydrogen and hydroxyl ions, which combine with the sodium ions and thus increase the concentration of sodium hydroxide in the catholyte. Typically, the outlet concentration of sodium hydroxide is around 32 wt.-%. A part of the product stream is diluted with demineralised water to about 30 wt.-% and used as catholyte inlet. In some units, a more diluted 23 wt.-% NaOH solution is produced. In these cases, the inlet concentration is adjusted to 20-21 wt.-%. Usually the NaOH solution is evaporated to the marketable concentration of 50 wt.-% using steam. Depleted brine leaving the anode compartment is saturated with chlorine and is therefore sent to a dechlorination unit to recover the dissolved chlorine before it is resaturated with salt for recirculation. The advantages of the membrane cell technique are the very high purity of the sodium hydroxide solution produced and the comparably low energy demand. Disadvantages comprise the high requirements on brine purity, the need for sodium hydroxide evaporation to increase concentration, and the comparably high oxygen content in the produced chlorine. In general, multiple cell elements are combined into a single unit, called electrolyser, of whom the design can be either monopolar or bipolar. In a monopolar electrolyser, the anodes and cathodes of the cells are connected electrically in parallel, whereas in the bipolar design, they are connected in series. Therefore, monopolar electrolysers require high current and low voltage, whereas bipolar electrolysers require low current and high voltage. Since bipolar systems allow higher current densities inside the cells, investment and operating costs are usually lower than for monopolar systems. References: Euro Chlor (2013) An Eco-profile and Environmental Product Declaration of the European Chlor-Alkali Industry, Chlorine (The chlor-alkali process). technologyComment of chlor-alkali electrolysis, mercury cell (RER, RoW): The mercury cell process comprises an electrolysis cell and a decomposer. Purified and saturated brine (25-28 wt.-% NaCl in water) is fed to the electrolysis cell on top of a film of mercury (Hg) flowing down the inclined base of the cell. The base of the cell is connected to the negative pole of a direct current supply forming the cathode of the cell. Anodes consisting of titanium coated with oxides of ruthenium and titanium are placed in the brine without touching the mercury film. At the anodes, chlorine gas is formed which is collected and directed to further processing. Due to a high overpotential of hydrogen at the mercury electrode, no gaseous hydrogen is formed; instead, sodium is produced and dissolved in the mercury as an amalgam (mercury alloy). The liquid amalgam is removed from the electrolytic cell and fed to a decomposer, where it reacts with demineralised water in the presence of a graphite-based catalyst to form sodium hydroxide solution and hydrogen. The sodium-free mercury is recirculated back into the cell. Cooling of hydrogen is essential to remove any water and mercury. The sodium hydroxide solution is very pure, almost free from chloride contamination and has usually a concentration of 50 %. Further treatment comprises cooling and removal of catalyst and mercury traces by centrifuges or filters. Advantages of the mercury cell process are the high quality of chlorine and the high concentration and purity of sodium hydroxide solution produced. The consumption of electric energy for electrolysis is, however, higher than for the other techniques and a high purity of the feed brine is required. Inherently, the use of mercury gives rise to environmental releases of mercury. References: Euro Chlor (2013) An Eco-profile and Environmental Product Declaration of the European Chlor-Alkali Industry, Chlorine (The chlor-alkali process).
Grundwassermessstellen dienen der Überwachung des Grundwassers. Dieser Datensatz enthält die Messdaten der Messstelle EVL LEV BR.2. Leiter: Niederterrasse Wasserart: reines Grundwasser
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