s/chemisches-gleichgewicht/Chemisches Gleichgewicht/gi
technologyComment of magnesium production, electrolysis (RoW, IL): Electrochemical processes to make magnesium are based on salts containing chloride which can be found naturally or are transformed from other raw materials like serpentine, magnesite, bischofite or carnallite. The magnesium chloride salts are dried with various processes in order to receive anhydrous MgCl2. The raw material for magnesium production in this activity is an anhydrous carnallite (MgCl2-KCl). In the process, KCl represents the electrolyte. In the course of the MgCl2 decomposition, the KCl content increases until the (spent) electrolyte is partly pumped out and replaced with new carnallite. Finally, two by-products are produced: liquefied chlorine (Cl2) and KCl-rich salt (70% KCl). Magnesium oxide (MgO) is formed as an impurity during dehydration. Concerning the CO2/CO equilibrium in the calcination process, there are numerous reactions that take place in the chlorination chambers and the carbon can be consumed by reaction with MgO, air, water, sulfates and other impurities. Theoretically, the predominant reactions are those in which carbon dioxide is formed. Thus, it is assumed that the carbon is entirely converted to CO2. The CO2 emissions from graphite anode consumption are expected to contribute less than 1 % of the overall emissions and are neglected in the module. In practice, the off gases are not released to the atmosphere as is, as they are treated in wet alkali scrubbers. That is that some of the CO2 (be it from the reaction or from the ambient dilution air) is converted to calcium carbonate. The input of petroleum coke contributes less than 1 % to the overall GWP results and is excluded from this datasets for reasons of confidentiality. technologyComment of magnesium production, pidgeon process (CN): The Pidgeon process includes the following process steps: calcination, grinding & mixing, briquetting, reducion and refining. Coal as energy source is only used in for the calcination process. For other process steps, coke oven, semi coke oven, producer or natural gas are used. The use of these fuels is calculated according to the weighted average in terms of annual magnesium output per fuel. The production of producer (coal) gas is included in this module. A main influencing factor for the emissions from fuel combustion is the composition of the fuel itself. Due to the different origins of the fuel gases used in the Pidgeon process, the composition of the gases varies considerably. For semi coke and coke oven gas, a large variation in gas composition can be observed. As the data base for these compositions is restricted to few measurements, no statistical average can be determined.
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 cyclohexane production (RER, RoW): Over 90 % of all cyclohexane is produced commercially by hydrogenation of benzene. A small amount is produced by superfractionation of the naphtha fraction from crude oil. Naturally occurring cyclohexane can be supplemented by fractionating methylcyclopentane from naphtha and isomerizing it to cyclohexane. Hydrogenation of benzene: Benzene can be hydrogenated catalytically to cyclohexane in either the liquid or the vapor phase in the presence of hydrogen. Several cyclohexane processes, which use nickel, platinum, or palladium as the catalyst, have been developed. Usually, the catalyst is supported, e.g., on alumina, but at least one commercial process utilizes Raney nickel. Hydrogenation proceeds readily and is highly exothermic (Δ H500K = – 216.37 kJ/mol). From an equilibrium standpoint, the reaction temperature should not exceed 300 °C. Above this, the equilibrium begins to shift in favor of benzene so that high-purity cyclohexane cannot be produced. As a result of these thermodynamic considerations, temperature control of the reaction is critical to obtaining essentially complete conversion of benzene to cyclohexane. Temperature control requires economic and efficient heat removal. This has been addressed in a number of ways by commercial processes. The earlier vapor-phase processes used multistage reactors with recycle of cyclohexane as a diluent to provide a heat sink, staged injection of benzene feed between reactors, and interstage steam generators to absorb the exothermic heat of hydrogenation. In the 1970s processes have been developed that use only one reactor or a combination of a liquid-and a vaporphase reactor. The objectives of the later processes were to reduce capital cost and improve energy utilization. However, all of the commercial processes have comparably low capital cost and good energy efficiency. In the vapor-phase process with multistage reactors in series, the benzene feed is divided and fed to each of the first two reactors. Recycled cyclohexane is introduced to the first reactor along with hydrogen. The recycled cyclohexane enables higher conversion in the reactors by absorbing part of the heat of hydrogenation. Steam generators between the reactors remove the heat of hydrogenation. The outlet temperature of the last reactor is controlled to achieve essentially 100 % conversion of benzene to cyclohexane. The effluent from the last reactor is cooled, and the vapor and liquid are separated. Part of the hydrogen-rich vapor is recycled to the first reactor, and the rest is purged to fuel gas or hydrogen recovery facilities. The liquid from the separator goes to a stabilizer where the overhead gas is sent to fuel gas; the remaining material is cyclohexane product, part of which is recycled to the first reactor. In the process with liquid- and vapor-phase reactors, benzene and hydrogen are fed to the liquid-phase reactor, which contains a slurry of finely divided Raney nickel. Temperature is maintained at 180 – 190 °C by pumping the slurry through a steam generator and by vaporization in the reactor. Roughly 95 % of the benzene is converted in this reactor. The vapor is fed to a fixed-bed reactor where the conversion of benzene is completed. The effluent from the fixed-bed reactor is processed as described previously for the vapor-phase process. Benzene hydrogenation is done typically at 20 – 30 MPa. The maximum reactor temperature is limited to ca. 300 °C so that a typical specification of < 500 mg/kg benzene and < 200 mg/kg methylcyclopentane in the product can be achieved. This is necessary because of the thermodynamic equilibrium between cyclohexane – benzene and cyclohexane – methylcyclopentane. Actually, equilibrium strongly favors methylcyclopentane, but the isomerization reaction is slow enough with the catalysts employed to avoid a problem if the temperature is controlled. The hydrogen content of the makeup hydrogen has no effect on product purity but it does determine the makeup, recycle, and purge gas rates. Streams with as low as 65 vol % hydrogen can be used. Carbon monoxide and sulfur compounds are catalyst deactivators. Both can be present in the hydrogen from catalytic naphtha reformers or ethylene units, which are typical sources of makeup hydrogen. Therefore, the hydrogen-containing stream is usually passed through a methanator to convert carbon monoxide to methane and water. Prior to methanation, hydrogen-containing gas can be scrubbed with caustic to remove sulfur compounds. Commercial benzene contains less than 1 mg/kg sulfur. In some cases, the recycle gas is also scrubbed with caustic to prevent buildup of hydrogen sulfide from the small amount of sulfur in the benzene. With properly treated hydrogen and specification benzene, a catalyst life in excess of three years can be achieved easily in fixed-bed reactors that use noble-metal catalysts supported on a base. The catalyst in the process that uses Raney nickel in suspension is reported to have a typical life of about six months before it must be replaced. Reference: Campbell, M. L. 2011. Cyclohexane. Ullmann's Encyclopedia of Industrial Chemistry.
Das Projekt "Balance and fate of heavy metals during the process of carbonisation of coal" wird vom Umweltbundesamt gefördert und von DMT-Gesellschaft für Forschung und Prüfung mbH durchgeführt. Objective: In view of their toxicity, trace elements (heavy metals) are receiving increasing attention in the context of both safety at work and environmental protection. As a result, they are the subject of various national and international regulations. However, very little is known abut the extent to which coking plants in the Community contribute to heavy metal pollution of the environment. The aim of the research project is to clarify this. General Information: The research will be carried out on a joint basis by the following four bodies: - Bergbau-Forschung GmbH (Federal Republic of Germany) - Centre de Recherches Metallurgiques (Belgium) - Laboratorie d'Etude et de Controle de l'Environnement Siderurgique (France) - National Smokeless Fuels Ltd (United Kingdom). Trace elements are to be measured: - in the incoming and outgoing material flows (coal, coke, tar, waste water, etc.), - in emissions, - at workplaces, - in the environment of coking plants. The plan of work is divided into a joint part in which (for example) methods of sampling and analysing trace elements are to be harmonized, and a specialized part in which Bergbau-Forschung will concentrate on emission measurement. Achievements: The project has been successful in the development and harmonisation of analytical methods between the participating organisations.
Das Projekt "Globales Klima und CO2: Die Rolle der Ozeanzirkulation" wird vom Umweltbundesamt gefördert und von Max-Planck-Institut für Meteorologie durchgeführt. Objective: To enhance our understanding of the role of ocean circulation changes in controlling the equilibrium concentration of carbon dioxide in the atmosphere. General information: The data from Cambridge and gif-sur-yvette will constitute an unique data base to compare with the simulations provided by the Hamburg ocean GCM. The modelling project planned by the MPI consists of the following activities: 1) computation of the mean ocean circulation for the various climatic epochs (18000 b.p., last glacial to interglacial transition, 125000 b.p.) using reconstructed or assumed boundary values as input data. 2) sensitivity studies to determine the sensitivity of computed ocean circulation states on boundary values (e.g. extent of sea ice, wind forcing, air temperature, fresh water influx from glacier) and on parametrization of physical processes (e.g. deep water formation). 3) repeat of the studies (1) and (2) with the ocean carbon cycle model to estimate earlier CO2 levels in the atmosphere and ocean, 13c/12c ratios,.....(the m.p.i. model is based on a 7 component carbon chemistry plus phytoplancton, detritus, nutrient and oxygen). 4) theoretical and numerical model studies of the interactions between ice sheets, ocean, atmosphere and the carbon cycle to ascertain the inherent stability or instability of the coupled system on a 10 3 to 10 5 time scale. These studies will include milankovitch and stochastic forcing. The goal is to test various published hypothesis and possibly gain new insights into the causes of climate variability on these time scales.
Das Projekt "Aufnahme und Nitrierung von Aromaten in der waessrigen Phase der Troposphaere" wird vom Umweltbundesamt gefördert und von Fraunhofer-Institut für Toxikologie und Aerosolforschung durchgeführt. General Information: The overall aim of the proposed project UNARO is to study tropospheric multiphase formation processes of nitroaromatic compounds which have been identified in field measurements of cloud and rain water and some of which are known to be toxic. To reach this aim within UNARO laboratory experiments on uptake and aqueous phase transformation mechanisms will be performed and combined with toxicologic studies in order to evaluate risk to human health. The project in detail focusses on the investigation of: - The uptake of polar aromatic hydrocarbons by aqueous solutions - Nitration reactions with NO3 radicals and nitronium ions in the aqueous phase and their products - Effectiveness of nitroaromatic formation pathways by including results into a two-box model - Toxicology and mutagenic activity of reaction products The chemical processing of organic molecules in aqueous atmospheric droplets is necessarily prefaced by transfer of the organic species from the gas to the aqueous phase. The rate of this transfer is controlled by five processes: 1) gas-phase diffusion to the droplet; 2) transfer across the gas/liquid interface described by the mass accommodation coefficient alpha; 3) liquid phase diffusion away from the interface; 4) reaction in the droplet; 5) gas-liquid phase equilibrium controlled by the Henry's Law coefficient, H. Diffusion is well understood and is readily calculated. Phase transfer, reactions in the droplets and gas-liquid phase equilibrium are of concern in this project. Alpha will be measured for phenol, 4-nitrophenol, p-cresol, 2-nitro-4-methylphenol and benzoic acid. The measurements will be made as a function of temperature and pH and ionic strength effects will also be checked. Experiments will be conducted with scavengers present to determine alpha directly. In order to better understand different pathways where nitration processes may occur within the tropospheric aqueous phase, experimental investigations are planned. - To study nitration reactions by the nitrate radical in aqueous solution. - To study nitration reactions by NO2+ in aqueous solution. - To perform product studies for the development of complete reaction pathways. Relevant nitration reactions to be studies (at various temperatures and ionic strengths) are: 1) Phenol to give nitration products: p-nitrophenol and 2,4-dinitrophenol. 2) p-Cresol to give nitration products: 2-nitro-4-methylphenol and 2,6-dinitro4-methylphenol. 3) Benzoic acid to give the nitration product 3-nitrobenzoic acid. 4) 4-methylbenzoic acid to give the nitration product 3-nitro-4-methylbenzoic acid. Atmospheric efficiency of nitroaromatic formation pathways will be assessed by directly including the measured parameters into a newly developed two-box model, where the gas phase chemistry is described by the RADM2 mechanism and coupled to a complex aqueous phase chemical mechanism. Prime Contractor:Univ. degli Studi di Milano, Dipartimento di Scienze dell'Ambientee del Ter
Das Projekt "Teilvorhaben: Bau und Betrieb einer Miniplant zur selektiven Ad- und Desorption von Kationen" wird vom Umweltbundesamt gefördert und von Fraunhofer-Einrichtung für Energieinfrastrukturen und Geothermie IEG durchgeführt. Gelöste Schwermetalle in Geothermalwässern wie z.B. Blei, Kupfer oder Barium neigen dazu, bei betriebsbedingten Veränderungen des chemischen Gleichgewichtes zu übersättigen und als schwerlösliche Verbindungen auszufallen. Die damit einher gehenden Probleme reichen von Verstopfung und Beschädigung von Installationen bis zu nachlassender Produktivität und Injektivität des Reservoirs und führen zu erhöhtem Wartungsaufwand oder gar Ausfall des Standortes. Um Partikelanreicherungen (Clogging) und Ausfällungen (Scaling) zu verringern wurden im Projekt PERFORM unterschiedliche Filtrationsmethoden entwickelt, die auf der Entfernung von scale-bildenden Schwermetallionen aus den Geothermalwässern basieren. Dabei wurden vielversprechende Ergebnisse mit Zeolith und Chitosanfasern als Filtrationsmittel im Labormaßstab erzielt. Hauptziel der geplanten Arbeiten in PERFORM II ist nun die Translation dieser Filter-Technologien in die industrielle Anwendung und deren Evaluierung unter geothermischen Bedingungen. Durch das IEG soll in diesem Zusammenhang eine Miniplant gebaut, in Betrieb genommen, und an verschiedenen Geothermiestandorten eingesetzt. Die Minianlage soll an den Standorten mit realen geothermalen Fluiden sowohl die Adsorptionsphase, als auch die Desorptionsphase durchlaufen. Hierbei sollen Kationen selektiv dem Eduktstrom entnommen und aus dem Filter abgeschieden werden. Die Anlage soll somit einen TRL von 6 bis 7 erreichen.
Das Projekt "Untersuchung der Einfluesse von Wasser- und Methanolzusaetzen auf den Wirkungsgrad sowie die Russ- und NOx-Emissionen des Dieselmotors" wird vom Umweltbundesamt gefördert und von Institut für Motorenbau Huber durchgeführt. Durch Zusaetze von Wasser und Methanol koennen die Schadstoffemissionen des Dieselmotors verringert werden. Die dabei auftretenden physikalischen und chemischen Wirkungsmechanismen sind im Hinblick auf einen gezielten und effektiven Einsatz dieser Zusaetze von besonderem Interesse. Zu deren Erforschung wurden drei Wege beschritten: 1. die Untersuchung der Einfluesse von Art, Ort und Zeitpunkt der Zugaben auf den Kraftstoffverbrauch und die Schadstoffemissionen des Motors; 2. die Aufnahme von Hochgeschwindigkeits-Farbschlierenfilmen zur optischen Darstellung der Wirkungen auf den Gemischbildungs- und Verbrennungsablauf; 3. die Berechnung der sich durch Wasser bzw. Methanol aendernden Verbrennungstemperaturen und Abgaszusammensetzungen auf der Basis von Reaktionsgleichgewichten. Wasser- und Methanolzugaben senken den kritischen lambda-Wert, bei dem die Russbildung einsetzt, so dass Russ erst bei groesserem Luftmangel zu entstehen beginnt. Der wesentlich staerkere Einfluss ist im Waermeentzug durch die Verdampfung zu sehen, der insbesondere bei Wasserzusatz den Zuendverzug und damit die Gemischbildungszeit verlaengert und die Verbrennungstemperatur absenkt. Dies fuehrt zu geringeren Rauchwerten und niedrigeren NO-Emissionen. Eine darueber hinausgehende Verbesserung der Gemischhomogenisierung durch vermeintliche Mikro-Explosionen konnte weder aus gezielten Motoruntersuchungen noch aus Filmaufnahmen festgestellt werden. Im Gegensatz dazu wird die Russverminderung durch Methanol im wesentlichen dadurch erreicht, dass es einen entsprechenden Anteil des Dieselkraftstoffes ersetzt und selbst russfrei verbrennt.
Das Projekt "Investigation of reactive halogen species in a smog chamber and in the field" wird vom Umweltbundesamt gefördert und von Universität Heidelberg, Institut für Umweltphysik durchgeführt. The objective of the proposed activities as part of the DFG research group HaloProc is the investigation of Reactive Halogen (RH) chemistry in the atmosphere by Differential Optical Absorption Spectroscopy. The importance of RH includes the destruction of ozone, change in the chemical balance, increased deposition of toxic compounds (like mercury) and potential indirect effects on global climate. In our laboratory experiments we observed events of 'Bromine Explosion' (auto catalytic release of reactive bromine from salt surfaces - key to ozone destruction) that were strongly dependent on pH and humidity. Our measurements from field campaigns in Namibia/Botsuana, Southern Russia and Mauritania during HaloProc1 showed 1 to 2 orders of magnitude lower BrO and IO levels than expected based on previous observations at salt flats. Environmental conditions might have strong influence, which would be consistent with the smog chamber studies. One of the main questions of the second phase is under which conditions RH activation take place does. It is of great interest whether reactions of chlorine and iodine compounds on salt surfaces are similar to those of bromine, and whether different RH compounds interact with each other. In addition, oxides of nitrogen might be important for their role in the reactivation of RH. Proposed field campaigns in Namibia and South Russia will allow us to investigate the sources, sinks and transformations of RH compounds. This work will be complemented by corresponding smog chamber experiments with measurements of different halogen oxides as well as photochemical model calculations.
Das Projekt "Teilvorhaben 1" wird vom Umweltbundesamt gefördert und von CUTEC-Institut GmbH durchgeführt. Bau und Betrieb eines Shift-Reaktors zur Einstellung des H2:CO-Verhältnisses in Synthesegasen aus Biomasse. Produkte sind Kraftstoffe der 2. Generation (BtL und Methan). Ziel bei BtL: Verbesserung des Wirkungsgrades der Gesamtkette; bei Methan: Ermöglichung des H2:CO-Verhältnis von 3. 1. Bau eines Labor- sowie eines Technikumsreaktors, 2. Optimierung von Katalysatoren des Partners H.C. Starck im Laborreaktor mit Flaschengasen. Im ersten Teil sind Katalysatoren für Synthesegase in die Fischer-Tropsch-Synthese zu optimieren; im zweiten Teil ein Synthesegas für die Methanisierung. 3. Versuchsbetrieb mit Synthesegasen aus Holz und Stroh im jeweils einwöchigen Dauerbetrieb für jede Katalysatormischung in einer vorhandenen Technikumsanlage zur Vergasung. 4. Kontinuierlicher Daten- und Erfahrungsaustausch mit Anlage in Güssing. 1. Steigerung des Wirkungsgrades des Gesamtkette bei BtL-Produktion notwendig für Bau kommerzieller Anlagen. 2. Produktion von Methan aus Biomasse mittels Vergasung ermöglicht neue Einsatzchancen landwirtschaftlicher Produkte u.v.a. von kohlenwasserstoffhaltigen Reststoffen. Verbundvorhaben enthält 1 Anlagenbauer, 1 Katalysatorproduzent, 1 Biomassekraftbetreiber.