The present study aimed at determining the influence of human activities on Antarctic soil-organisms communities as well as the potential introduction of non-native species into Antarctic habitats. In the Antarctic summers of the years 2009/2010 and 2010/2011, soil organisms (plants and the soil fauna of the groups Nematoda, Tardigrada, Collembola, Actinedida, Oribatida and Gamasina) were collected from anthropogenically influenced and non-influenced areas of the total of 13 localities and compared Veröffentlicht in Texte | 22/2013.
EDC is produced industrially by the chlorination of ethylene, either directly with chlorine or by using hydrogen chloride (HCl). In practice, both routes are carried out together, the HCl stems from the cracking of EDC to vinyl chloride. HCl from other processes can also be used. The major outlet is for the production of vinyl chloride monomer (VCM). There are both integrated EDC / VCM plants as well as stand-alone EDC plants. In 1997, European production of EDC was 9.4 million tons, according to (IPPC Chemicals, 2002). This makes it Europe’s most produced halogenated product. Global demand is expected to grow at roughly 6% per year in the short run, while future growth depends on the global demand for PVC. Major plants with capacities greater than 600’000 tons per year are located in Belgium, France, the Netherlands, Italy, Norway, the US, Canada, Brazil, Saudi Arabia, Japan and Taiwan. Available data from production sites often refer to the entire EDC/VCM chain and do not differentiate between the production lines. There is some information on stand-alone sites, however, and this data forms the basis for part of the inventory developed in this report. EDC can be produced by two routes, both involving the chlorination of ethylene. One route involves direct chlorination, the other is carried out with hydrochloric acid (HCl) and oxygen. In practice, both routes are carried out together. This study includes an average of the available literature data from both routes. EDC by direct chlorination of ethylene: C2H4 + Cl2 C2H4Cl2 Yield on ethylene 96-98% / on chlorine 98% Liquid chlorine and pure ethylene are reacted in the presence of a catalyst (ferric chloride). The chlorination reaction can be carried out at low or high temperature. In the low-temperature process takes place at 20 ºC – 70 ºC. The reaction is exothermic and heat exchangers are needed. The advantage of this process is that there are few by-products. The high-temperature process takes place at 100 ºC – 150 ºC. The heat generated is used to distill the EDC, which conserves energy. the reaction product consists of more than 99% EDC, the rest being chlorinated hydrocarbons that are removed with the light ends and then combusted or sold. EDC by direct chlorination of ethylene: C2H4 + Cl2 C2H4Cl2 Yield on ethylene 96-98% / on chlorine 98% Liquid chlorine and pure ethylene are reacted in the presence of a catalyst (ferric chloride). The chlorination reaction can be carried out at low or high temperature. In the low-temperature process takes place at 20 ºC – 70 ºC. The reaction is exothermic and heat exchangers are needed. The advantage of this process is that there are few by-products. The high-temperature process takes place at 100 ºC – 150 ºC. The heat generated is used to distill the EDC, which conserves energy. Tthe reaction product consists of more than 99% EDC, the rest being chlorinated hydrocarbons that are removed with the light ends and then combusted or sold. EDC by chlorination and oxychlorination: C2H4 + Cl2 C2H4Cl2 (1) C2H4 + 1/2 O2 + 2HCl C2H4Cl2 + H2O (2) Yield on ethylene 93-97% / on HCl 96-99% Pure ethylene and hydrogen chloride are heated and mixed with oxygen. The reaction occurs at 200 ºC – 300 ºC at 4-6 bar in the presence of a catalyst (cupric chloride). After reaction the gases are quenched with water. The acid and water are removed, the gases are cooled and the organic layer is washed and dried. If air is used instead of oxygen, the reaction is easier to control. However, oxygen-based processes operate at lower temperatures, reducing vent gas volume. By-products are ethyl chloride, 1,1,2-trichloromethane and chloral (trichloroacetaldehyde). Thermal cracking of EDC: Thermal cracking of dry, pure EDC produces VCM and HCl. Often all the HCl generated in the cracking section is reused in producing EDC by oxychlorination. Plants that exhibit this characteristic and also do not export EDC are called “balanced”. The balanced process is the common process used as a Best Available Technology benchmark. C2H4 + Cl2 C2H4Cl2 (Chlorination of ethylene to EDC) C2H4Cl CH2CHCl + HCl (Cracking of EDC to form VCM) C2H4 + 1/2 O2 + 2HCl C2H4Cl2 + H2O (Oxychlorination route to EDC) Reference: IPPC Chemicals, 2002 European Commission, Directorate General, Joint Research Center, “Reference Document on Best Available Techniques in the Large Volume Organic Chemical Industry”, February 2002 Wells, 1999 G. Margaret Wells, “Handbook of Petrochemicals and Processes”, 2nd edition, Ashgate, 1999
Das Projekt "Almeria solar powered reverse osmosis plant" wird vom Umweltbundesamt gefördert und von DaimlerChrysler Aerospace AG durchgeführt. Objective: To demonstrate, that small scale PV powered water desalination plants can be constructed in a compact and cost efficient way. This type of plant is urgently needed in Southern Europe and Developing Countries. Intensive publicity is intended and good commercialisation is expected (100 systems potential market in Spain only). General Information: On the site of the ALMERIA university, brackish water is pumped from a well of 60m. Drinking water (about 8000 cbm per year) obtained by a reverse osmosis plant is stored for consumption. A 23.5 kWp PV generator supplies the required energy. Number of subsystems: 1 Power of subsystems: 23.5 kWp Total power: 23.5 kWp Module description: 612 AEG type PQ 10/20/01;(Typ I) + 306 AEG type PQ 10/40/01;(T.II) (I): 20 10x10cm poly crist. cells, 6 V,16.5 W (II): 40 10x10cm poly crist. cells, 12 V,38.4 W Very high resistance glass; UV stabilized PVB; 6.7 kg; 0.25 or 0.5 sqm. Connections: type 20: 36 series, 17 parall.: type 40: 18 series, 17 parall. Support: on racks Max. power tracker: included in inverter Charge controller: charge/discharge regulator: special design, microprocessor controlled. Battery: Spanish TUDOR, 110 cells Battery Volt.: 220 V; Battery capacity: 2240 Ah.(at 100 h). (1650 Ah (10h); type C 10 Battery capacity: 493 kWh.(at 100 h). Inverter: (for well water pump only): AEG, Solarverter, type SV3 sinusoidal, transistor-pulse type, 3 kHz. Input nominal: 130 to 300 V DC in; max 16 A Dc; Output nominal: 3.3 kVA; 13 to 127 V out; 3 phases; to 50/60 Hz. Load description: PLEUGER submersible pump NE612 for raw water pumping. (three phase, AC motor, hence inverter necessary). 4.2 cbm/h, header 30 m. Rated power 2.2 kW. ROCHEM (Hamburg) reverse osmosis, type RORO 1535-B 709165; presses raw water through membrane. Input: 92 cbm/day at 7000 ppm; Output: 60 cbm/day at smaller than 500 ppm. New type of PLATE MODULE system, with turbulent flow on the feed water side and hence less membrane scaling and fouling which leads to less maintenance. The pressure pump of the RO system works with 220 V DC motor, 6750 W, avoiding inverters. Monitoring: Weather station; Reading every 10 seconds six relevant plant data, averaging over ten minutes, storing on floppy. (DAM 800 data acquisition system by TELEFUNKEN). Stored data: (1) Insolation, array plane. (2) amb. temp. (3) module temp. (4) array output energy. (5) energy to and from battery. (6) inverter dc energy. Achievements: While the pv generator and the batteries worked without problem the water pumps, the reverse osmosis plant, the inverter and the monitoring system had several, partly major, failures. The Final Report on System Monitoring (5 June 95) analyses 32 month of operation and puts in evidence: the system is well designed for its task; however the frequent failures of some components decrease its effective utilisation. The plant will continue to operate after the end of the project with some improvements (new pumps, new membranes, etc.)...
Das Projekt "Mercury oxidation activity of used SCR-DeNOx catalysts of a coal-fired power plant" wird vom Umweltbundesamt gefördert und von Universität Magdeburg, Institut für Apparate- und Umwelttechnik, Professur für Umweltschutztechnik durchgeführt. The Hg-oxidation activity of catalyst samples from the four levels of a SCR-DeNOx plant operated in a coal-fired power plant was to be determined. The activity was to be evaluated under DeNOx-inactive operation condition (NH3/NO =0) in the absence and presence of SO2 and under DeNOx-active condition (NH3/NO =0.9) in the absence of SO2. The activity data are part of the catalyst management strategy of the DeNOx plant for the next two operation years.
Das Projekt "An eco-innovative planting and survival support system for urban trees (TREEPAD)" wird vom Umweltbundesamt gefördert und von H. Lorberg Baumschulerzeugnisse GmbH & Co.KG durchgeführt.
Das Projekt "The Demonstration of Waste Biomass to Synthetic Fuels and Green Hydrogen (TO-SYN-FUEL)" wird vom Umweltbundesamt gefördert und von Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung eingetragener Verein durchgeführt. TO-SYN-FUEL will demonstrate the conversion of organic waste biomass (Sewage Sludge) into biofuels. The project implements a new integrated process combining Thermo-Catalytic Reforming (TCR©), with hydrogen separation through pressure swing adsorption (PSA), and hydro deoxygenation (HDO), to produce a fully equivalent gasoline and diesel substitute (compliant with EN228 and EN590 European Standards) and green hydrogen for use in transport . The TO-SYN-FUEL project consortium has undoubtedly bought together the leading researchers, industrial technology providers and renewable energy experts from across Europe, in a combined, committed and dedicated research effort to deliver the overarching ambition. Building and extending from previous framework funding this project is designed to set the benchmark for future sustainable development and growth within Europe and will provide a real example to the rest of the world of how sustainable energy, economic, social and environmental needs can successfully be addressed. This project will be the platform for deployment of a subsequent commercial scale facility. This will be the first of its kind to be built anywhere in the world, processing organic industrial wastes directly into transportation grade biofuels fuels which will be a demonstration showcase for future sustainable investment and economic growth across Europe. This project will mark the first pre-commercial scale deployment of the technology processing up to 2100 tonnes per year of dried sewage sludge into 210,000 litres per year of liquid biofuels and up to 30,000 kg of green hydrogen. The scale up of 100 of such plants installed throughout Europe would be sufficient to convert up to 32 million tonnes per year of organic wastes into sustainable biofuels, contributing towards 35 million tonnes of GHG savings and diversion of organic wastes from landfill. This proposal is responding to the European Innovation Call LCE-19.
Das Projekt "Rational supply of power, heat and cooling buildings demonstation by a hospital in Dresden" wird vom Umweltbundesamt gefördert und von DBI Gas- und Umwelttechnik GmbH durchgeführt. Objective: The overall objective of this project is to demonstrate the optimized combination of innovative technologies and equipment such as fuel cell operating on natural gas, adsorption refrigeration machine, new type of solar collectors, PV-System and highly efficient air conditioning technology at the hospital of the 'Malteser Betriebsträgergesellschaft Sachsen GmbH' in Kamenz (DE). The primary aim is to apply renewable energy sources and rational use of energy in order to reduce the annual fossil fuel and electricity consumption by an estimated total of 2.0x10exp6 KWH/Y. The estimated payback period is 9.3 years based on a total investment of 3016477 ECU of which the Commission may provide support up to 783000 ECU. The project is estimated to take 3.1 years in total to complete all phases, and additional benefits will include an estimated reduction per annum of CO2 440 ton (demonstration object in Kamenz), and a decline in noise and dust pollution. General Information: A demonstration plant will be installed in Germany (Hospital of the 'Malteser Betriebsträgergesellschaft Sachsen GmbH' in Kamenz). The hospital will be located nearly the town Kamenz (Eastern Saxon region). The location is a part of the place Kamenz (land register sections 153g,h,i,j,k,l,m and 153-16). The total area is 30520 m , the effective area is 20200m . The hospital will have a capacity of 210 sickbeds and a day-hospital (psychiatry) for 20 patients. In addition to air-conditioning and refrigeration requirements, the heat demand for room and water heating shall be met. in the demonstration plant, a fuel cell for combined heat and power generation and an adsorption plant are used. The fuel cell will provide not only the base load for the adsorption machine and heating but also a part of the power supply to the building. The peak-load of the adsorption machine will be covered by solar collectors. In the project planning phase, computer simulations using simulation software TRNSYS are carried out, by means of which the demand for the different forms of energy will be optimised for the demonstration plant. Installation and implementation of the plant are followed by the measurement phase (about 2 years), the result of which will be optimization of the individual systems and the whole system. Highly efficient air-conditioning technology will operate in the building using a minimum of primary energy as a result of cooling ceilings combined with DEC1 equipment in the ventilation plant. An adaptive, self learning control system will be integrated into the plant. On the basis of the detailed weather forecast, this system determines the respectives actual energy demand for air-conditioning and heating in a sliding and predictive way, and accordingly adapts the mode of plant operation. Considerable energy savings are expected, in particular, as a result of the predictive operation of heating and air-conditioning.
Das Projekt "Treatment of electrolytes from a zinc electrolysis plant by eed (electro-electro-dialysis)" wird vom Umweltbundesamt gefördert und von Preussag-Weser-Zink durchgeführt. Objective: To build and operate a dialysis cell of industrial size together with the necessary ancillary equipment to test the EED process in long term commercial use. The EED allows a higher yield of zinc connected with considerable energy savings for removal of magnesium from the electrolyte compared with alternative possibilities. General Information: Preussag-Weser-Zink GmbH operates in Nordenham (Germany) a plant for the hydrometallurgical-electrolytic production of zinc with a capacity of 110 000 tons of electrolytic zinc per year. During the electrolysis an enrichment of the magnesium content of the electrolyte taken place. To limit this enrichment, a special treatment of a part of the electrolyte stream is necessary. Per ton of produced zinc generally 0.1 to 0.2 m3 of electrolyte are subjected to this treatment which consists of neutralizing the electrolyte with zinc. This leads to the formation of 30 to 70 Kg per ton of produced zinc, which is costly and energy intensive to dispose of. Within the framework of this project it is intended to subject a part of the magnesium containing neutral zinc sulfate (neutral lye) as a catholyte to an Electro-Electro-Dialysis (EED). In the EED more than 80 per cent of the zinc is separated in the usual quality at the cathode while a corresponding part of sulfate ions go into the anolyte and arerecirculated into the process. The zinc which has and been separated at the cathode in the EED is recovered in a second process step by selective precipitation. EED was developed in the research institute of Minemet in France and pilot testing took place at Preussag-Weser-Zink GmbH, during 12 months. The pilot plant consisted of 2-3 dialysis cells producing daily 3 Kg of zinc per cell. Results from the pilot trials confirmed the previous laboratory work. The demonstration plant consisted of a dialysis cell with five industrially sized cathodes of 1,2 m2 active surface and additional equipment for the treatment of the catholyte by selective precipitation. The production capacity of the demonstration plant was 50 kg zinc per day. From the laboratory work and the previous pilot tests for a 110,000. For a 110,000 tons zinc producing plant the estimated energy saving amounts to 1,400 TOE/year, in addition to which 91 000 000 000 KJ/a of primary energy are substituted with 32.3 000 000 000 KJ/a of electrical energy. On the basis of the above saving, the cost of handling 1 m3 of the electrolyte solution is calculated to be DM 168. compared to the current disposal cost (to a third party) of DM 198. The process is covered by a joint patent and a cooperation contract covers the relationship between Minemet and Preussag. Achievements: Important technical know-how for electrolytic processes using membranes was generated. Among others the cell with compartments for cathodes and anodes and the membranes fixing system had to be designed and materials and membranes chosen. The membrane IONAC MA 3475 from SYBRON CHEMICALS gave...
Das Projekt "3,5-MW-Waermepumpensystem fuer die Rueckgewinnung von Abwaerme aus Malzdarrprozessen" wird vom Umweltbundesamt gefördert und von Malzfabrik Weißheimer durchgeführt. Objective: The project was intended to reduce the energy input for malt drying at the Friedrich Weissheimer Malzfabrik plant at Gelsenkirchen from 67000 MWh a year to 44 000 MWh a year. General Information: The proposal was to install two heat pumps with inputs of 330 kw and 420 kw. These would draw water from the harbour next to the plant through the evaporator system and heat would be transferred via r22 and r12 refrigerant circuits operated by five sabroe smc 16l compressors. The system was planned to operate as a bivalent system, the temperature being boosted through the existing boiler heating plant. Water heat was exchanged in an air heater and this circuit was used to dry the malt in the malt kilns. The plant output was approximately 90 000 tonnes of malt a year which required about 92 000 mwh a year for drying. About 25000 Mwh were available via the existing heat recovery system. The heat pump installation was planned to contribute a further 23000 Mwh a year for the use of approximately 5 500 Mwh a year of electricity. The system was the result of considerable investigation and planning by messes. Weissheimer in association with Dr.-Ing. Harald Steinhaus of Att Energietechnik. The project, which was a refinement of previous suggestions to use an electricity powered heat pump system, was particularly attractive because harbour water at a relatively high temperature designed for 18 deg.C was available. The Gelsenkirchen site was near other industrial premises, particulary a refinery. Emission from these premises raised the water temperature locally. The system was built and installed during the latter half of 1981 and the beginning of 1982. The main heat pump installation was the responsibility of Sabroe Kältetechnik GmbH of Flensburg. The targets were to integrate the system during the first half of 1982 and operate the demonstration programme between June-July 1982 and June-July 1983. In the event a series of problems meant that the plant was not judged to be properly integrated into the malt production process until July 1983. Achievements: At the beginning of August 1983, the heat pump system had to be taken out of operation owing to an evaporator fault which turned out to be irreparable. The cause of the corrosion damage to the evaporator could not to be fully ascertained, although it soon became evident that replacement in the original (copper) material was not to be considered. Since it was not possible to recommission the plant in its original form (due to the high cost) it was decided to convert the heat pump system to use waste heat from the refrigeration systems. By optimising the integration of the heat pump system into the production process it was possible to increase the number of hours of its operation from +/- 18 h/d in 1982 to +/- 22 h/d in mid-1983. As a result of restrictions in the available power supply (+/- 2500 kW) useful heat pump output was around 2 to 3 MW on simultaneous operation of the refrigeration ...
Das Projekt "Energy savings by improvement of combustion air preheating by means of an upstream heat exchanger" wird vom Umweltbundesamt gefördert und von ThyssenKrupp Stahl AG durchgeführt. Objective: Use of low temperature waste heat for additional preheating of the combustion air and for prevention of low temperature corrosion. This technique yields an increase of the plant availability and a longer life of the recuperator by preventing the temperature from falling below the dew point to prevent corrosion. Innovative aspects: concept first realization. Long testing and measurement period to assess energy saving and efficiency and payback time. General Information: In industrial furnaces a part of the heat from the flue gas is used to pre-heat the combustion air. When intensive use is made of the heat from the flue gas, there is frequently a great drop in temperature to below the dew point. When the fuel gases are loaded with aggressive materials, the passing of the dew point causes low temperature corrosion on heat exchanger components. As a result of this, the heat exchanger is increasingly destroyed which entails constant worsening of efficiency very rare (once to twice per year) with some plants, i.e. reheating furnaces in the steel industry, so that more fuel is consumed over a long period because of defective air pre-heating insulation and the environment is thus burdened more than is required with an intact installation. A heat exchanger for a thermal capacity of 1.0 MW is to be erected upstream of the reheating furnace of a rolling mill fired by sulphur bearing coke oven gas. The energy for a pre-heating is taken from the skid rail cooling circuit which has a temperature level of maximum 90 deg. C