Ziel: Ermittlung der oekologischen Effizienz von wasserbaulichen Aufstiegsanlagen in Fliessgewaessern fuer Wirbellose und Fische. Ergebnisse: Technische Aufstiegsanlagen sind wegen Verstopfungsgefahr und Unterhaltungsaufwand eher ungeeignet. Rauhe Rampen sind guenstige Aufstiegsanlagen, wie die Wiederfaenge von markierten Fischen und Wirbellosen beweisen. Natuerliche/naturnahe Umgehungsbaeche sind sehr geeignete Wanderwege. Das Gefaelle im Bauwerk sollte mindestens 1:20 betragen. Ruheraeume und natuerliche Anschluesse an Oberwasser und Unterwasser muessen favorisiert werden. Lueckige Sohlsubstrate und Uferstrukturen beguenstigen den Aufstieg.
Arbeitsschwerpunkt dieses Teilprojektes ist in AP4 die Probenahme zur Quantifizierung des MP-Aufkommens und -Transports im realen, urbanen Abwassersystem für die Abwasserfraktionen Niederschlagswasser, häusliches Schmutzwasser (Teilströme Grau- und Schwarzwasser) und betriebliches Schmutzwasser durch die TU Kaiserslautern. Dabei werden die Erkenntnisse zur Probenentnahme aus AP 2 umgesetzt und methodisch weiter verwertet. Weitere Arbeitsschwerpunkte sind die Probenaufbereitung und -konservierung sowie relevanzabhängig die abgestufte Analyse ausgewählter Standard-Abwasserparameter zwecks Bewertung der Vergleichbarkeit unterschiedlicher Probennahmestrategien. Die Untersuchungen sind im Schwerpunkt auf die Mengen und die Bedeutung der MP-Aufkommen in den einzelnen Eintragspfaden des urbanen Abwassersystems auf das Umweltkompartiment Gewässer ausgerichtet. Als Vorhabensziele sind zu nennen: a) Erprobung und Modifikation der entwickelten Probennahmestrategien am realen Abwassersystem, b) Relevanzbewertung verschiedener Eintragspfade von MP-Frachten, c) Entwicklung ganzheitlicher Probennahmestrategien für das gesamte Abwasserinfrastruktursystem d) Abschätzung von MP-Aufkommensspektren, sowie e) Erkenntnisgewinn zur MP-Analytik (u.a. Wiederfindungsraten in heterogenen Abwasserproben mit ausgeprägten Matrixeffekten, Korrelation mit weiteren Abwasserparametern).
Ziel ist es, die Qualität der GRACE Level-1 und Level-2 Produkte zu verbessern und GRACE Schwerefelder gegen in-situ Ozeanbodendruck zu validieren. Um dieses Ziel zu erreichen werden Methoden entwickelt, die eine realistische Einschätzung der Genauigkeit sowie eine optimale Prozessierungsstrategie zur Generierung der in die Prozessierung einfließenden Level-1B Produkte beinhalten. Um das Produkt zur Modellierung von kurzzeitigen Massenvariation in Atmosphäre und Ozeanen zu verbessern, soll die zeitliche Auflösung erhöht, die Behandlung von Atmosphärengezeiten optimiert und ein baroklines Ozeanmodell weiterentwickelt und implementiert werden. Ebenfalls ist geplant, tägliche hydrologische Variationen einzubeziehen. Diese verbesserten Level-1 Produkte werden mit globalen und regionalen Methoden zu alternativen Schwerefeldprodukten verarbeitet und anschließend gegen in-situ Ozeanbodendruckdaten validiert. Dazu sollen Ozeanbodendruckrekorder ausgelegt und möglichst viele Ozeanbodendruckdaten beschafft werden. Die Ergebnisse werden für die Basis-Prozessierung im wissenschaftlichen Prozessierungszentrum für die GRACE-Mission verwendet.
Objective: To save energy by recovering the heat contained in the acidic fumes at temperatures below their dew-point and emanating from the drying operation of a bleaching powder plant. The air heated by the recovered heat will be fed back into the drying oven, saving an estimated 327 TOE/yr of primary energy. The novelty in this process consists in the use of ''Teflon'' as a corrosion-resistant coated on the heat exchanger. A 3 years payback is to be expected at project level. General Information: In the Moosburg plant, bleaching powder is produced by treating aluminium ore with hot HCl (hydrochloric acid). The hydrochloric residues are then air-dried in ovens, from which air exists at a rate of 200,000 m3/hr and at a temperature of 110 degree C, close to the dew-point. Part of this chlorine-containing (60,000 m3/hr or 48,000 kg/hr with 21 per cent of steam) is fed into a heat-exchanger built of glass-tubes in stainless steel casings (tubes and plates), coated internally with PTFE (Teflon). The air tightness between the tubes and plates will be provided by metallic gaskets coated with PFA, a highly thermal and chemical resistant material. The two airflows will move in counter-current, with the air to be preheated flowing inside the tubes. The primary air, cooled to 70 degree C, will flow to a humidifier for washing and then be released in the atmosphere. For a 38,000 kg/hr flow of air preheated from 20 degree C to 76 degree C during an annual 6,500 hours operation, a saving of 13 970GJ/year of natural gas can be achieved. From this, the electricity to operate two additional fans i.e. 130,000 Kwh/year must be substracted, leaving a net saving of 13 500 GJ/year, equivalent to 327 TOE/year. The heat recovery will be measured in 12 monthly recordings of temperature and flow. The pressures, dew-points and water consumptions will be equally monitored by the 30st June 1987. Achievements: During the preliminary start-up, several deficiencies were found in connection to the PFTE lining of the heat exchanger, the optimum function of the mist eliminator and the increased discharges of drips from the chimney due to condensate formation in the chimney waste-gas-stack. To avoid these defects, several actions were taken including repairs, coupling of dust eliminator and modification leading a partial quantity of the produced warm air into the waste-gas-stack. These modifications caused a 29 per cent cost increased and a 25 per cent decrease in actual energy economy measured. The equipment reliability is still to be proved during the measurement campaign.
Objective: This project was first presented as EE./00225/85/DE (no Sesame sheet issued). Recovery of the expansion energy of natural gas by means of a low cost modified steam turbine. General Information: Modified single stage steam turbine coupled to an asynchronous generator of 500 kW nominal output. Expansion of 48 million m3/year from 45 to 1.5 bar, producing 1964 MWh/y of electric power. 65 per cent of necessary preheating is covered by waste heat, 35 per cent by gas fired boiler. Innovation: use of modified low cost steam turbine for recovery of expansion energy of natural gas.
Objective: Maintaining the product quality when applying the continuous heating process, and evaluation of the savings. General Information: In the conventional process the wort is boiled for about 90 to 150 min. in a brewing kettle; at the same time as various chemical reactions are going on, water is evaporated. After separation of hop residues and albumen, the wort is cooled down, then yeast is mixed ; the wort is then fermented and seasoned until the actual beer is ready. The main feature of the process is to separate the individual process steps such as wort heating, reaction and water evaporation, in order to reduce energy costs by heat recovery. The wort is fed at 75 deg. C from a feed tank into a pre-heater where it is heated to 95 deg. C by steam. Final heating up to 120 deg. C takes place in a live steam heat exchanger. The wort flows through a residence section where the necessary reaction takes place without evaporation. Then the required evaporation is done in a 4 stage flash column. Then the wort is cooled down in a plate heat exchanger. The heat released from the vapours produced in the first flashing stage of the column is used in the heat exchanger in order to preheat the wort. The vapours of the other flash stages are condensed in the condensers and heat the brewing water up to 80 deg. C. The vapour condensate is cooled down to below 30 deg. C. Having reached this temperature, the condensate is directly discharged. Change-over to a different beer is simply achieved by displacing the wort with hot water and then displacing this with the new wort. Monitoring of energy consumption was done with the 'CAPO' data acquisition system between the end of December 1985 and middle of July 1986. Achievements: In January 1985, tests had to be stopped due to corrosion and subsequent leakage in the four heat exchangers. Attempts were made to continue operation until delivery of new heat exchangers. Despite repairs one of the exchangers began to leak with a consequent mixing of vapour condensate and brewing water. It was then decided to operate the system by isolating the leaking exchanger and with only two exchangers to heat the brewing water. Although difficult, this proved possible. Evaporation was limited to 8 per cent (max) and major fluctuations in the control loops had to be avoided. Brewing water temperature was maintained at 80 deg.C. As evaporation was limited to 8 per cent max. a premise and exact operation was required when producing the primary wort. The only disadvantage is that malt extract losses must be expected. The Hannen brewery opted for the Heidelberg process due to its promise of low (comparatively) energy consumption, although a higher evaporation rate of 10 per cent is necessary to guarantee known high standards. However, up to the end of the period under review (ending 12.2.86) it was not possible to verify the energy savings which may be obtained with an evaporation rate of 10 per cent. However, the quality ...
Objective: The project is to develop, manufacture, and test a sampling and measuring device for the continuous determination of mercury and its compounds in the flue gas of incineration plants. In addition, the sampling device will be capable of collecting other heavy metals, such as arsenic, cadmium, chromium, lead, copper, manganese, and nickel. Mercury will be determined photo metrically. The detection limit for Hg is approximately 2 mug/m3. The tests will take place in the industrial environment of a municipal waste incineration plant. The basic principle of the device has been patented. General Information: Mercury (Hg) and its compounds are highly toxic chemicals; emissions from plants, such as waste incinerators, should be prevented as far as possible. Typically, filters are used in order to remove the remaining emissions; for new municipal refuse incineration plants, the EC Directive 89/369 limits Hg emissions after the filters to 200 mug/m3. A device for the continuous control of Hg has been recently developed by the Essen-based VEREWA MESS- UND REGELTECHNIK GMBH. The EC Commission assisted the development and testing of an industrial-environment measuring device at 50 per cent of the project costs. The Hg measuring device consists of a sampling and the measuring part proper. The isokinetic sampling device is capable of sampling not only Hg but other heavy metals as well, such as Cu, Ni, Zn, Sn, Sb, Ba, Pb, Mn. The average Hg retrieval statistics is approximately 93 per cent. The measuring device proper determines the Hg concentration in the dried flue gas by UV AA photometry, the detection limit is approximately 2 mug/m3. The measuring device may be calibrated at any time, allowing for the check of the zero and reference points and of the linearity of the device. Idle time between each taking is in the range of ms; the measured values are shown on the monitor every 2 seconds; the measuring protocols may average the values to convenience. Overall standard deviations are approximately 5 per cent; thus, the device can be used for process control. Further extensions of the measuring device are possible to allow for the determination of heavy metals other than Hg as well. The device has been successfully tested and optimized for several months in the heavy-duty industrial environment of the flue gas stack of a municipal waste incineration plant. Working entirely automatically, the device meets the need for a reference device for the control of emissions from refuse incinerators, as stipulated by the EC Directive 89/369. Achievements: A device for the continuous control mercury has been recently developed. The measuring device consists of a sampling part and the measuring part proper. The isokinetic sampling device is capable of sampling not only mercury but other heavy metals as well, such as copper, nickel, zinc, tin, antimony, barium, lead and manganese. The average mercury retrieval is approximately 93 per cent...
Objective: The objective is better recovery of nickel from slags through better process control in order to raise productivity and save energy in ferronickel production. General Information: An automatic process control system will be developed for the recovery of mechanical nickel losses in slag arising from the production of ferronickel in the electric reduction furnace of LARCO at the Larymna plant. Methodological development will help applicability to other comparable processes. The project will be in the following stages. Construction and setup of a dedicated induction furnace with a graphite susceptor and a refractory crucible and with the possibilities of temperature control and gas injection from the top or from the side of the crucible. The development of a laser based system for assessing and monitoring the metal content of the slag is proposed. The proposed system, laser induced breakdown spectroscopy (LIBS), will speed up the analysis of the recovery of metal, provide more efficient process control and enable further optimization. The basic steps in LIBS are: atomization of the sample; excitation of the resulting atoms; and detection of the emitted radiation from the atoms. Both atomization and excitation can be achieved by focusing a neodymium, yttrium aluminium garnet(YAG) laser on the molten slag free surface, resulting in the creation of a microplasma. The emitted radiation will be spectrally resolved by means of a monochromator coupled with an optical multichannel analyzer (OMA III). The work parts to be done are: preliminary measurements on solid slag containing nickel and ferronickel in order to be used as reference standards; online monitoring with data acquisition and sensor system integration for the actual molten systems; testing and validation; and metallurgical support during the experiments. The control system stage will involve: metal concentration values given by the LIBS system modelled to obtain the actual metal content in the slag; thermal control linked with the process computer; control of the gas (or gas mixtures) flow rates to be injected into the slag melt linked with the process computer. The information processing stage will involve: observed values continuously stored in an appropriate database in order to be compared to the simulated values; special, easy to solve, mathematical model of ordinary differential equations developed to simulate the recovery process; and a simulation programme developed in advanced continuous simulation language (ACSL) to allow online simulation. The final stage is system integration. Achievements: Research was carried out in order to develop an automatic process control system for the recovery of metal from slags and therefore contribute with better process control to better recovery of the mechanical metal losses from the ERF slags in the ferronickel production. The combination of metallurgical experiments with the high technology of laser based analysis was the first ...
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