Die Extraktion anorganischer Komponenten aus Böden ergibt aus ihrer Untersuchung eine spezielle Form bodenanalytischen Daten. Es handelt sich um bodenchemische Daten. Sie werden im Labor des LUNG M-V erhoben (Meß-Rohdaten, kombinierte Daten, Meßreihen, statistische Aussagen über Daten). Sie sind verteilt abgelegt in Laborbüchern, Rohdatenfiles der Meßgeräte, Spreadsheet-Daten. Es existieren Daten zu den Extraktionsmitteln Doppellactat, Dithionit, Reinstwasser, Oxalat, Calciumchlorid, Strontiumchlorid und Azetaten.
Die Fa. Swarco Limburger Lackfabrik GmbH beabsichtigt in der Gemarkung Diez, Flur 35, Flurstück 187 die wesentliche Änderung einer bestehenden Anlage zur Herstellung von Anstrich- oder Beschichtungsstoffen (Lasuren, Firnis, Lacke, Dispersionsfarben) oder Druckfarben unter Einsatz von 25 t oder mehr je Tag an flüchtigen organischen Verbindungen, die bei einer Temperatur von 293,15 Kelvin einen Dampfdruck von mindestens 0,01 Kilopascal haben. Gegenstand der geplanten Maßnahme • ist die Änderung der gehandhabten Stoffe in den Behältern o HB 10 (16 m³) Lagerung von Domacryl 935 (entzündbare Flüssigkeit H225) o HB 11 (16 m³) Lagerung von Domacryl 935 (entzündbare Flüssigkeit H225) o TL 7 (16 m³) Lagerung von Methylisobutylketon (entzündbare Flüssigkeit H225) o TL 8 (16 m³) Lagerung von Methylisobutylketon (entzündbare Flüssigkeit H225) o TL 12 ((9) (30 m³) Lagerung von Glycol Ether PM Acetat (entzündbare Flüssigkeit H226) • sind 3 zusätzliche Aggregate in der BE 08 Produktion Bunt- und Sonderfarben o Sendebehälter Pb8 o Dissolver D5 o Dissolver D6 • ist die Errichtung und der Betrieb einer mobilen Abluftreinigungsanlage (Aktivkohlefilter). Die genehmigte Produktionskapazität der Anlage wird durch die geplanten Maßnahmen nicht geändert.
Wesentliche Änderung einer Anlage zur Herstellung von Stoffen oder Stoffgruppen durch chemische, biochemische oder biologische Umwandlung in industriellem Umfang zur Herstellung von sauerstoffhaltigen Kohlenwasserstoffen wie Alkohole, Aldehyde, Ketone, Carbonsäuren, Ester, Acetate, Ether, Peroxide, Epoxide nach Nr. 4.1.2 des Anhangs 1 der 4. BImSchV durch den Austausch der bestehenden Anlage zur Abluftbehandlung mittels Aktivkohlefilter mit einer Anlage zur thermischen Nachverbrennung sowie der künftigen Verwendung von Triethylphosphat als Flammschutzmittel in der Gemarkung Oberroßbach, Flur 7, Flurstücke 109/9 sowie 75/1
Wesentliche Änderung einer Anlage zur Herstellung von Stoffen oder Stoffgruppen durch chemische, biochemische oder biologische Umwandlung in industriellem Umfang zur Herstellung von sauerstoffhaltigen Kohlenwasserstoffen wie Alkohole, Aldehyde, Ketone, Carbonsäuren, Ester, Acetate, Ether, Peroxide, Epoxide nach Nr. 4.1.2 des Anhangs 1 der 4. BImSchV in der Gemarkung Oberroßbach, Flur 7, Flurstücke 109/9 sowie 75/1
Die Firma OQ Chemicals Produktion GmbH & Co. KG, Paul-Baumann-Straße 1 in 45772 Marl hat die Genehmigung zur wesentlichen Änderung und zum Betrieb der Acetate- und Harzfabrik zur Herstellung von Acetaten und Harz auf dem Grundstück Paul-Baumann-Straße 1 in 45772 Marl (Gemarkung Marl, Flure 53, 63, Flurstücke 15, 30, 129) beantragt. Gegenstand des Antrages ist die Umsetzung von Maßnahmen aus dem überarbeiteten Sicherheitskonzept und die Erhöhung der Kapazität von 4.000 t/a auf 6.000 t/a Harze.
Production mix technologyComment of decarboxylative cyclization of adipic acid (RER): decarboxylative cyclization of adipic acid technologyComment of formic acid production, methyl formate route (RER): The worldwide installed capacity for producing formic acid was about 330 000 t/a in 1988. Synthesis of formic acid by hydrolysis of methyl formate is based on a two-stage process: in the first stage, methanol is carbonylated with carbon monoxide; in the second stage, methyl formate is hydrolyzed to formic acid and methanol. The methanol is returned to the first stage. Although the carbonylation of methanol is relatively problem-free and has been carried out industrially for a long time, only recently has the hydrolysis of methyl formate been developed into an economically feasible process. The main problems are associated with work-up of the hydrolysis mixture. Because of the unfavorable position of the equilibrium, reesterification of methanol and formic acid to methyl formate occurs rapidly during the separation of unreacted methyl formate. Problems also arise in the selection of sufficiently corrosion-resistant materials Carbonylation of Methanol In the two processes mentioned, the first stage involves carbonylation of methanol in the liquid phase with carbon monoxide, in the presence of a basic catalyst: imageUrlTagReplacea0ec6e15-92c8-4d44-82bb-84e90e58b171 As a rule, the catalyst is sodium methoxide. Potassium methoxide has also been proposed as a catalyst; it is more soluble in methyl formate and gives a higher reaction rate. Although fairly high pressures were initially preferred, carbonylation is carried out in new plants at lower pressure. Under these conditions, reaction temperature and catalyst concentration must be increased to achieve acceptable conversion. According to published data, ca. 4.5 MPa, 80 °C, and 2.5 wt % sodium methoxide are employed. About 95 % carbon monoxide, but only about 30 % methanol, is converted under these circumstances. Nearly quantitative conversion of methanol to methyl formate can, nevertheless, be achieved by recycling the unreacted methanol. The carbonylation of methanol is an equilibrium reaction. The reaction rate can be raised by increasing the temperature, the carbon monoxide partial pressure, the catalyst concentration, and the interface between gas and liquid. To synthesize methyl formate, gas mixtures with a low proportion of carbon monoxide must first be concentrated. In a side reaction, sodium methoxide reacts with methyl formate to form sodium formate and dimethyl ether, and becomes inactivated. The substances used must be anhydrous; otherwise, sodium formate is precipitated to an increasing extent. Sodium formate is considerably less soluble in methyl formate than in methanol. The risk of encrustation and blockage due to precipitation of sodium formate can be reduced by adding poly(ethylene glycol). The carbon monoxide used must contain only a small amount of carbon dioxide; otherwise, the catalytically inactive carbonate is precipitated. Basic catalysts may reverse the reaction, and methyl formate decomposes into methanol and carbon monoxide. Therefore, undecomposed sodium methoxide in the methyl formate must be neutralized. Hydrolysis of Methyl Formate In the second stage, the methyl formate obtained is hydrolyzed: imageUrlTagReplace2ddc19c0-905f-42c3-b14c-e68332befec9 The equilibrium constant for methyl formate hydrolysis depends on the water: ester ratio. With a molar ratio of 1, the constant is 0.14, but with a water: methyl formate molar ratio of 15, it is 0.24. Because of the unfavorable position of this equilibrium, a large excess of either water or methyl formate must be used to obtain an economically worthwhile methyl formate conversion. If methyl formate and water are used in a molar ratio of 1 : 1, the conversion is only 30 %, but if the molar ratio of water to methyl formate is increased to 5 – 6, the conversion of methyl formate rises to 60 %. However, a dilute aqueous solution of formic acid is obtained this way, and excess water must be removed from the formic acid with the expenditure of as little energy as possible. Another way to overcome the unfavorable position of the equilibrium is to hydrolyze methyl formate in the presence of a tertiary amine, e.g., 1-(n-pentyl)imidazole. The base forms a salt-like compound with formic acid; therefore, the concentration of free formic acid decreases and the hydrolysis equilibrium is shifted in the direction of products. In a subsequent step formic acid can be distilled from the base without decomposition. A two-stage hydrolysis has been suggested, in which a water-soluble formamide is used in the second stage; this forms a salt-like compound with formic acid. It also shifts the equilibrium in the direction of formic acid. To keep undesirable reesterification as low as possible, the time of direct contact between methanol and formic acid must be as short as possible, and separation must be carried out at the lowest possible temperature. Introduction of methyl formate into the lower part of the column in which lower boiling methyl formate and methanol are separated from water and formic acid, has also been suggested. This largely prevents reesterification because of the excess methyl formate present in the critical region of the column. Dehydration of the Hydrolysis Mixture Formic acid is marketed in concentrations exceeding 85 wt %; therefore, dehydration of the hydrolysis mixture is an important step in the production of formic acid from methyl formate. For dehydration, the azeotropic point must be overcome. The concentration of formic acid in the azeotropic mixture increases if distillation is carried out under pressure, but the higher boiling point at high pressure also increases the decomposition rate of formic acid. At the same time, the selection of sufficiently corrosion-resistant materials presents considerable problems. A number of entrainers have been proposed for azeotropic distillation. Reference: Gräfje, H., Körnig, W., Weitz, H.-M., Reiß, W.: Butanediols, Butenediol, and Butynediol, Chapter 1. In: Ullmann's Encyclopedia of Industrial Chemistry, Sev-enth Edition, 2004 Electronic Release (ed. Fiedler E., Grossmann G., Kersebohm D., Weiss G. and Witte C.). 7 th Electronic Release Edition. WileyInterScience, New York, Online-Version under: http://www.mrw.interscience.wiley.com/ueic/articles/a04_455/frame.html technologyComment of oxidation of butane (RER): The liquid-phase oxidation of hydrocarbons is an important process to produce acetic acid, formic acid or methyl acetate. About 43 kg of formic acid is produced per ton of acetic acid. Unreacted hydrocarbons, volatile neutral constituents, and water are separated first from the oxidation product. Formic acid is separated in the next column; azeotropic distillation is generally used for this purpose. The formic acid contains about 2 wt % acetic acid, 5 wt % water, and 3 wt % benzene. Formic acid with a content of about 98 wt % can be produced by further distillation. Reference: Gräfje, H., Körnig, W., Weitz, H.-M., Reiß, W.: Butanediols, Butenediol, and Butynediol, Chapter 1. In: Ullmann's Encyclopedia of Industrial Chemistry, Sev-enth Edition, 2004 Electronic Release (ed. Fiedler E., Grossmann G., Kersebohm D., Weiss G. and Witte C.). 7 th Electronic Release Edition. WileyInterScience, New York, Online-Version under: http://www.mrw.interscience.wiley.com/ueic/articles/a04_455/frame.html
technologyComment of acetaldehyde oxidation (RER, RoW): Oxidation of acetaldehyde technologyComment of acetic acid production, product in 98% solution state (RER, RoW): The process represents the Celanese process (which is an optimized version of the Monsanto process) in which methanol reacts with carbon monoxide under the influence of a rhodium catalyst. It is assumed that 50% of the off-gas is burned as fuel, thus VOC emissions are reduced and CO2 is higher. References: Le Berre, C., Serp, P., Kalck, P. and Torrence, G. P. 2014. Acetic Acid. Ullmann's Encyclopedia of Industrial Chemistry. technologyComment of oxidation of butane (RoW): Oxidation of butane technologyComment of oxidation of butane (RER): The liquid-phase oxidation of hydrocarbons is an important process to produce acetic acid, formic acid or methyl acetate. About 43 kg of formic acid is produced per ton of acetic acid. Unreacted hydrocarbons, volatile neutral constituents, and water are separated first from the oxidation product. Formic acid is separated in the next column; azeotropic distillation is generally used for this purpose. The formic acid contains about 2 wt % acetic acid, 5 wt % water, and 3 wt % benzene. Formic acid with a content of about 98 wt % can be produced by further distillation. Reference: Gräfje, H., Körnig, W., Weitz, H.-M., Reiß, W.: Butanediols, Butenediol, and Butynediol, Chapter 1. In: Ullmann's Encyclopedia of Industrial Chemistry, Sev-enth Edition, 2004 Electronic Release (ed. Fiedler E., Grossmann G., Kersebohm D., Weiss G. and Witte C.). 7 th Electronic Release Edition. WileyInterScience, New York, Online-Version under: http://www.mrw.interscience.wiley.com/ueic/articles/a04_455/frame.html
Im Teilvorhaben 'Entwicklung Laminationstechnologie' des Verbundvorhabens 'Gepard' soll Anlagen- und Prozesstechnologie zur Senkung der spezifischen Modulherstellungskosten (in €/Wp) entwickelt werden. Als Schlüssel dazu wird eine Laminationstechnologie weiterentwickelt mit dem Ziel die Laminationszeit signifikant zu verkürzen, die Lamination von sphärisch gewölbten PV-Modulen zu ermöglichen sowie eine inlinefähige Charakterisierung des EVA-Vernetzungsgrades (ethylene-vinyl acetate copolymer) zu implementieren.
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