Geophysical methods are essential for exploration and monitoring of subsurface formations, e.g. in carbon dioxide sequestration or enhanced geothermal energy. One of the keys to their successful application is the knowledge of how the measured physical quantities are related to the desired reservoir parameters. The work presented in this thesis shows that the presence of carbon dioxide (CO2) in pore space gives rise to multiple processes all of which contribute to the electrical rock conductivity variation. Basically, three mechanisms take place: (1) CO2 partially replaces the pore water, which is equivalent to a decrease in water saturation. (2) CO2 chemically interacts with the pore water by dissolution and dissociation. These processes change both the chemical composition and the pH of the pore filling fluid. (3) The low-pH environment can give rise to mineral dissolution and/or precipitation processes and changes the properties of the grain-water interface. Investigations on the pore water phase show that the reactive nature of CO2 in all physical states significantly acts on the electrical conductivity of saline pore waters. The physico-chemical interaction appears in different manifestations depending mainly on the pore water composition (salinity, ion types) but also on both temperature and pressure. The complex behaviour includes a low- and a high-salinity regime originating from the conductivity increasing effect of CO2 dissociation, which is opposed by the conductivity decreasing effect of reduced ion activity caused by the enhanced mutual impediment of all solutes. These results are fundamental since the properties of the water phase significantly act on all conduction mechanisms in porous media. In order to predict the variation of pore water conductivity, both a semi-analytical formulation and an empirical relationship for correcting the pore water conductivity, which depends on salinity, pressure and temperature, are derived. The central part of the laboratory experiments covers the spectral complex conductivity of water-bearing sand during exposure to and flow-through by CO2 at pressures up to 30MPa and temperatures up to 80°C. It is shown that the impact of CO2 on the real part of conductivity of a clean quartz sand is dominated by the low- and high-salinity regime of the pore water. The obtained data further show that chemical interaction causes a reduction of interface conductivity, which could be related to the low pH in the acidic environment. This effect is described by a correction term, which is a constant value as a first approximation. When the impact of CO2 is taken into account, a correct reconstruction of fluid saturation from electrical measurements is possible. In addition, changes of the inner surface area, which are related to mineral dissolution or precipitation processes, can be quantified. Both the knowledge gained from the laboratory experiments and a new workflow for the description and incorporation of geological geometry models enable realistic finite element simulations. Those were conducted for three different electromagnetic methods applied in the geological scenario of a fictitious carbon dioxide sequestration site. The results show that electromagnetic methods can play an important role in monitoring CO2 sequestration. Compared to other geophysical methods, electromagnetic techniques are generally very sensitive to pore fluids. The proper configuration of sources and receivers for a suitable electromagnetic method that generates the appropriate current systems is essential. Its reactive nature causes CO2 to interact with a water-bearing porous rock in a much more complex manner than non-reactive gases. Without knowledge of the specific interactions between CO2 and rock, a determination of saturation and, consequently, a successful monitoring are possible only to a limited extend. The presented work provides fundamental laboratory investigations for the understanding of the electrical properties of rocks when the reactive gas CO2 enters the rock-water system. All laboratory results are put in the context of potential monitoring applications. The transfer from petrophysical investigations to the planning of an operational monitoring design by means of close-to-reality 3D FE simulations is accomplished.

No description available.

Geophysical methods are essential for exploration and monitoring of subsurface formations, e.g. in carbon dioxide sequestration or enhanced geothermal energy. One of the keys to their successful application is the knowledge of how the measured physical quantities are related to the desired reservoir parameters. The work presented in this thesis shows that the presence of carbon dioxide (CO2) in pore space gives rise to multiple processes all of which contribute to the electrical rock conductivity variation. Basically, three mechanisms take place: (1) CO2 partially replaces the pore water, which is equivalent to a decrease in water saturation. (2) CO2 chemically interacts with the pore water by dissolution and dissociation. These processes change both the chemical composition and the pH of the pore filling fluid. (3) The low-pH environment can give rise to mineral dissolution and/or precipitation processes and changes the properties of the grain-water interface. Investigations on the pore water phase show that the reactive nature of CO2 in all physical states significantly acts on the electrical conductivity of saline pore waters. The physico-chemical interaction appears in different manifestations depending mainly on the pore water composition (salinity, ion types) but also on both temperature and pressure. The complex behaviour includes a low- and a high-salinity regime originating from the conductivity increasing effect of CO2 dissociation, which is opposed by the conductivity decreasing effect of reduced ion activity caused by the enhanced mutual impediment of all solutes. These results are fundamental since the properties of the water phase significantly act on all conduction mechanisms in porous media. In order to predict the variation of pore water conductivity, both a semi-analytical formulation and an empirical relationship for correcting the pore water conductivity, which depends on salinity, pressure and temperature, are derived. The central part of the laboratory experiments covers the spectral complex conductivity of water-bearing sand during exposure to and flow-through by CO2 at pressures up to 30MPa and temperatures up to 80°C. It is shown that the impact of CO2 on the real part of conductivity of a clean quartz sand is dominated by the low- and high-salinity regime of the pore water. The obtained data further show that chemical interaction causes a reduction of interface conductivity, which could be related to the low pH in the acidic environment. This effect is described by a correction term, which is a constant value as a first approximation. When the impact of CO2 is taken into account, a correct reconstruction of fluid saturation from electrical measurements is possible. In addition, changes of the inner surface area, which are related to mineral dissolution or precipitation processes, can be quantified. Both the knowledge gained from the laboratory experiments and a new workflow for the description and incorporation of geological geometry models enable realistic finite element simulations. Those were conducted for three different electromagnetic methods applied in the geological scenario of a fictitious carbon dioxide sequestration site. The results show that electromagnetic methods can play an important role in monitoring CO2 sequestration. Compared to other geophysical methods, electromagnetic techniques are generally very sensitive to pore fluids. The proper configuration of sources and receivers for a suitable electromagnetic method that generates the appropriate current systems is essential. Its reactive nature causes CO2 to interact with a water-bearing porous rock in a much more complex manner than non-reactive gases. Without knowledge of the specific interactions between CO2 and rock, a determination of saturation and, consequently, a successful monitoring are possible only to a limited extend. The presented work provides fundamental laboratory investigations for the understanding of the electrical properties of rocks when the reactive gas CO2 enters the rock-water system. All laboratory results are put in the context of potential monitoring applications. The transfer from petrophysical investigations to the planning of an operational monitoring design by means of close-to-reality 3D FE simulations is accomplished.

Im Rahmen der vorliegenden Arbeit wurden verschiedene duroplastische Formmassen laboranalytisch hinsichtlich der rheologischen und thermischen Eigenschaften untersucht. Es wurde u.a. gezielt die absolute Materialfeuchte gesteigert, um den Einfluss dieser auf das Fließ­ Härtungsverhalten zu charakterisieren. Anschließend wurden die Materialien auf einer hochinstrumentierten Spritzgussmaschine mit einem Fließspiralenwerkzeug untersucht. Dabei konnte ein direkter Zusammenhang zwischen dem Rückfluss und dem Plastifizierdrehmoment in Abhängigkeit der Materialfeuchte und der Prozessparameter detektiert werden . Des Weiteren wurden über die Differenzdruckmessung im Fließspiralenwerkzeug die scheinbaren Viskositäten über den Fließweg ermittelt. Hierbei konnten unterschiedliche Aufschmelzeffekte über die Fließweglänge in Abhängigke it der duroplastischen Formmasse, der absoluten Materialfeuchte und der Prozessparameter detektiert werden . Durch Schererwärmung konnte die Formmassentemperatur teilweise die Werkzeugtemperatur übersteigen. Hinsichtlich der mechanischen Eigenschaften (Schlagzähigkeit, Biegefestigkeit) konnten keine signifikanten Einflussgrößen detektiert werden. Hinsichtlich des Tg konnten systematischen Unterschiede detektiert und begründet werden. Die beste Möglichkeit zur Ermittlung des Tg lieferte die TMA. Die thermischen Glasübergänge korrelieren mit den in der DSC ermittelten Aushärtegraden , wobei mit steigender Materialfeuchte ein geringer Aushärtegrad detektiert wird. / Within this paper, the rheologieal and thermie eharaeteristies of different thermosetting molding eompounds were investigated using lab analysis methods. Among others, the absolute moisture eontent was inereased purposefully to investigate its influenee on the flow-euring behavior. Subsequently, the materials were analyzed using a highly instrumented injeetion-molding maehine and a flow spiral tool. A direet link between the baekflow and the plastifieation torque dependent on the moisture eontent and proeess parameters was deteeted . Furthermore, a measurement of the differential pressure was eondueted within the flow spiral to deteet the apparent viseosity over the flow path. Within this proeess, different melting effeets over the flow eurve length depending on the molding eompound, the absolute moisture eontent and proeess parameters were deteeted. The shear heating lead to a material temperature inerease of the molding eompound, whieh was partly higher than the tool temperature . Coneerning the meehanieal eharaeteristies (impaet strength, flexural strength), no signifieant influeneing faetors eould be deteeted. In eontrast, systematie differenees of the glass transition temperature were deteeted and their eause eould be explained. The best way to determine the glass transition is the TMA. The glass transition temperatures eorrelate with the degree of eure determined with the DSC, whereas an inereasing moisture eontent is assoeiated with a lower degree of eure.

In this work, atomic scale investigation of pressure-induced transformations in the solid state have been carried out. A series of compounds including GaN, ZnO, CaF2, and AgI, in addition to elemental phosphorus have been studied. The corresponding transition mechanisms have been elucidated with a clear description of atomic displacements and intermediate structures involved therein. In the first group of compounds, the long standing debate on the transition path of the wurtzite(WZ)-to-rocksalt(RS) transition in semiconductors, GaN and ZnO was resolved using geometrical modeling combined with molecular dynamics (MD) simulations conducted in the frame of transition path sampling (TPS) method. In GaN, a two-step mechanism through a metastable intermediate phase with a tetragonal structure iT has been revealed from simulations. In ZnO, the tetragonal intermediate structure was kinetically less stable, although still part of the real transition mechanism. It appeared at the interface between WZ and RS as consequence of a layers shearing. The transition regime in ZnO was characterized by a competition between iT structure and another hexagonal intermediate with hexagonal symmetry iH. Although possible, the latter is not functional for the transition. In both cases, GaN and ZnO, two points of agreement with experiments have been revealed. The tilting of structures after transition, and the phonon mode softening associated with atomic displacements leading to the tetragonal structure iT In the second group of compounds, the investigation of transitions in superionic conductors, CaF2 and AgI, demonstrated a different and particular behavior of atomic motion under pressure. The solid-solid reconstruction of CaF2 structure was shown to be initiated and precedented by high disorder of the anionic sublattice. The percolation of fluoride ions through voids in the fluorite structure created a thin interface of liquid like state. The sparce regions caused by the departure of anions facilitates the cation sublattice reconstruction. In AgI, ion diffusion during the wurtzite/zincnlende(ZB)$rocksalt transition was more pronounced due to the extended stacking disorder WZ/ZB. The Ag+ ions profited not only from the structure of the interface but used the combination of interstitial voids offered by both phases, WZ and ZB, to achieve long diffusion paths and cause the cation sublattice to melt. Clearly, a proper account for such phenomena cannot be provided by geometry-designed mechanisms based on symmetry arguments. In phosphorus, the question of how the stereochemically active lone pairs are reorganized during the orthorhombic (PI) to trigonal (PV) structural transition was answered by means of simulations. Computation was performed at different levels theory. First, the mechanism of the transition was obtained from TPS MD simulations. MD runs were performed within density functional tight binding method (DFTB). The analysis of atomic displacements along the real transformation path indicated a fast bond switching mechanism. In a second step, the nature of the interplay between orbitals of phosphorus during the bond switching was investigated. A simultaneous deformation of lone pair and P−P bond showed a mutual switching of roles during the transformation. This interplay caused a low dimensional polymerization of phosphorus under pressure. The corresponding structure formed as zigzag linear chain of fourfold coordinated phosphorus atoms (· · ·(P(P2))n · · ·) at the interface between PI and PV phases. A further result of this work was the development of a simulation strategy to incorporate defects and chemical doping to structural transformations. On top of the transition path sampling iterations, a Monte Carlo like procedure is added to stepwise substitute atoms in the transforming system. Introducing a chemically different dopant to a pure system represents a perturbation to the energy landscape where the walk between different phases is performed. Therefore, any change in the transition regime reflects the kinetic preference of a given structural motif at times of phase formation. This method was applied to the elucidation of WZ-RS transition mechanism in the series of semiconducting compounds AlN, GaN, and InN. Simulations showed that In atoms adopt the same transformation mechanism as in GaN and favor it, while Al atoms demonstrated a significant reluctance to the path going through tetragonal intermediate iT. The difference between transition regime in mixed systems InxGa1−xN and AlxGa1−xN is in agreement with experiments on high pressure behavior of AlN, GaN, and InN. While transitions in GaN and InN are reversible down to ambient conditions, AlN is stable. The work presented in this thesis constitutes the seed of new perspectives in the understanding of pressure-induced phase transformations in the solid state, where the physics and the chemistry are brought together by means of computer simulations.

With this thesis, I present an experimental study focusing on the provision of thermodynamic data of fluids at elevated pressure and temperature conditions. Hereby a microcapillary setup that is equipped with an in situ Raman Spectroscopy unit as well as with a high-speed camera, was further improved within the scientific employment of the author. The setup consists in principle of a fused-silica microcapillary embedded in a heating block, which is furthermore connected to high pressure syringe pumps. Pure compounds and mixtures were studied with the microfluidic setup and different thermodynamic properties were determined. For instance, vapor pressures of Poly(oxymethylene) Dimethyl Ethers (OME3 and OME4), a potential class of renewable diesel fuels, were the first time measured for temperatures exceeding the atmospheric boiling temperature. Hereby the regarded compound is pressurized at constant temperature, from what the vapor pressure is determined optically by detecting bubble or film formation, indicating the transition from vapor to liquid state. The main results of this thesis were however the vapor-liquid equilibria (VLE) of fuel/air-systems that were determined by in situ Raman Spectroscopy, whereby the Stokes-scattered Raman signal can be successfully separated phase-dependently by light barrier technology. A further task was the determination of saturated mixture densities of the validation system ethanol/CO2. With this study, I intend to contribute to the scarce literature data for the studied systems and properties. Therewith I want to help to enhance the understanding of microprocesses such as the evaporation and mixing formation in diesel combustion engines.

In dieser Arbeit werden folgende Arbeiten vorgestellt: ● Aufbau eines Schockwellenlabors für unterschiedliche Einsatzzwecke für eine Nettoexplosivmasse von bis zu 20 kg, bezogen auf NSH 711 (C4 nach MIL-Standard), ● Klärung der Ursachen des Probenverlustes bei Schockwellensyntheseexperimenten ab Überschreitung eines gewissen materialabhängigen Grenzdruckes unter Verwendung von in der Literatur vorgegebenen Standardmethoden sowie eine wissenschaftlich fundierte Prob-lembehebung auf der Basis empirischer Theorien, ● Berechnung der Zustandsgrößen Druck (p), Temperatur (T) sowie Zeit (t) unter den ge-wählten Versuchsbedingungen für unterschiedliche Problemstellungen und Materialien mit Kontrollmöglichkeiten sowie ● Gewährleistung des maximal möglichen Phasenumwandlungsgrades für die entsprechende Hochdruckphase. Insgesamt wurden im Verlauf der Entwicklungsarbeiten im Schockwellenlabor 122 Spren-gungen durchgeführt. Die Drücke betragen dabei zwischen 15 GPa und ca. 180 GPa. Es gelangen zahlreiche erfolgreiche Synthesen der Hochdruckphasen gamma-Si3N4 sowie rs-AlN mit Probenmengen von 0,2g bis zu 7,3g Hochdruckphase pro Versuch. Es wurden auf Basis der Rankine-Hugoniot-Zustandsgleichung drei empirische Grundprinzipien der Schockwellensynthese entwickelt, welche es nunmehr gestatten, die Schockwellenversuche reproduzierbar sowie gut kontrollierbar zu gestalten. Dies sind die „Vermeidung von Mach-Effekten“, die „Impedanzkorrektur der Probeneinheit“ sowie die „Kontrolle der adiabatischen Dekompression“. In mehr als 100 Experimenten, welche mit der impedanzkorrigierten Probeneinheit durchgeführt wurden, trat in keinem Fall Probenverlust auf, Gasdichtheit konnte teilweise hergestellt werden. Dies war unabhängig von dem erreichten Druck oberhalb des technisch bedingten Mindestdruckes von 15 GPa innerhalb der Probeneinheit möglich. Es wurden Versuche sowohl mit der Reflektionsmethode als auch mit der Impedanzmethode durchgeführt sowie für besondere Experimente dünne Metallplatten zwischen Flugplatte und Containeroberseite verwendet. In allen genannten Fällen sind die unterschiedlichen Druck- und Temperaturbedingungen in den Proben eindeutig verifizierbar. Weiterhin gelang es im Rahmen dieser Arbeit erstmals, sowohl Calciumcarbonat als auch Kaolinit (sogenannte fluidreiche Phasen) bis in den Druckbereich p> 100 GPa unter unterschiedlichen Temperaturen dynamisch zu belasten, ohne dass die empfindlichen Proben Ent-gasungs- bzw. Zerfallserscheinungen (Calcit) bzw. Aufschmelzungen (Kaolinit) aufwiesen. Besonderes Augenmerk ist dabei auf die Schocktemperatur zu richten, um den Druckaufbau nicht durch eine zu starke Aufheizung der Probe zu reduzieren (sogenanntes Knudson-Problem). Jede zukünftige Erhöhung des Druckes macht gleichzeitig eine Reduzierung der relativen Schocktemperatur erforderlich. Diese experimentellen Erfolge sind lediglich in dem Falle möglich, wenn im Schockwellenlabor folgende Grenzbedingungen eingehalten werden: ● Die Schockgeschwindigkeit Us ist größer als die Schallgeschwindigkeit des betreffenden Stoffes. ● Die erzielten Drücke sind höher als das Hugoniot-Elastic-Limit des betreffenden Stoffes und somit im Bereich des plastischen Verhaltens. ● Die maximale Porosität k des Impedanzpulvers ist kleiner als die Mie-Grüneisen-Grenze des betreffenden Stoffes. ● Die maximalen Drücke sind geringer als der Bulk-Modulus des betreffenden Stoffes und die Schallgeschwindigkeit im dichten Medium ist größer als die Schockgeschwindigkeit (Bereich der so genannten „schwachen Schockwellen“). ● Es wird ein Impedanzpulver-Probe-Verhältnis von >9:1 verwendet. ● Weiterhin stellt für die Schockwellensyntheseexperimente unter Vermeidung der freien adiabatischen Dekompression die Schocktemperatur (die Temperatur im Bereich des konstanten Druckes) die ausschlaggebende Größe dar. Für die Berechnung wurde entschieden, die Software MatLab zu verwenden. Die Berechnungen folgen den Grundlagen der linearen Algebra. Für die Berechnung der Zustandsgleichung wurden im Rahmen dieser Arbeit folgende vereinfachende Annahmen verifiziert: ● Unter den genannten Bedingungen gilt der lineare Zusammenhang zwischen Partikelge-schwindigkeit Up und Schockgeschwindigkeit Us. ● Unter den Bedingungen des Freiberger Schockwellenlabors sind die Unterschiede zwischen der gespiegelten Hugoniot und der release-adiabat-Kurve sehr gering, es kann an deren Stelle die gespiegelte Hugoniot verwendet werden. ● Die maximalen Drücke sind niedriger als der Schmelzpunkt auf der Hugoniot, sämtliche in dieser Arbeit dargestellten Berechnungen betreffen die beteiligten Stoffe im festen Zustand. Die impedanzkorrigierte Probeneinheit ist nicht zum Messen von Zustandsgleichungen geeignet, die Methoden „vollständige Probenrückgewinnung“ sowie „Messung der Zustands-gleichung“ schließen sich gegenseitig aus.:Motivation 1 1 Einführung 5 1.1 Das Hochdruckforschungszentrum (FHP) der Dr. Erich-Krüger-Stiftung 5 1.2 Möglichkeiten zur Erzeugung hoher dynamischer Drücke sowie zur Schockwel-lensynthese 24 1.3 Aufgaben des neuen Schockwellenlabors in Freiberg 31 2 Aufbau und Betrieb des neuen untertägigen Schockwellen- labors der TU Bergakademie Freiberg 35 2.1 Sprengarbeiten unter Bergrecht an einer Hochschule 35 2.2 Rechtliche Situation des Schockwellenlabors an der TU Bergakademie Freiberg 39 2.3 Lage und Dimensionierung des Schockwellenlabors 47 2.4 Ausrüstung des Labors 51 3. Physikalische Grundlagen 58 3.1 Verwendete Sprengstoffe 58 3.2 Detonation des Sprengstoffes und die Rankine-Hugoniot- Zustandsgleichung 60 3.2.1 Die Druck-Partikelgeschwindigkeits-Beziehung 64 3.2.2. Die Beziehung zwischen Druck und Differenz der spezifischen Volumina 66 3.2.3. Die Beziehung zwischen Druck und Differenz der spezifischen Inneren Energien 67 3.3 Plane-Wave-Generator (PWG) mit Flyer-Plate 69 3.3.1. Aktiver PWG 73 3.3.2. Passiver PWG 73 3.4 Beschleunigung der Flugplatte 74 3.5 Kollision der Flugplatte mit dem Probencontainer 77 3.6 Mie-Grüneisen-EoS und die Berechnung der Schocktemperatur 82 3.7 Verdichtung poröser Materialien 89 3.8 Schockwellenreflektionen 94 3.8.1 Reguläre Reflektionen 95 3.8.1.1 Reflektion an einer freien Oberfläche sowie adiabatische Dekompression 95 3.8.1.2 Reflektion an einer Materialgrenze 99 3.8.2 Irreguläre Reflektionen (Mach-Effekte) 102 3.9 Impedanzmethode 103 3.10 Reflektionsmethode beziehungsweise „ramp compression“ 107 3.11 Phasenumwandlungen aus schockwellenphysikalischer Sicht 112 4. Detaillierter Aufbau der Versuchsanordnung sowie Funktion der Einzelbestandteile 115 4.1 Versuchsanordnung 115 4.2 Explosiveinheit mit PWG und Arbeitsladung 116 4.2.1 Plane-Wave-Generator 116 4.2.2 Arbeitsladung 120 4.2.3 Flugplatte 122 4.2.4 Schaumstoffeinlage 123 4.2.5 Distanzring 124 4.2.6 Beschleunigung der Flugplatte 124 4.3. Probeneinheit 127 4.3.1 Probencontainer 129 4.3.2 Cu-Folie 131 4.3.3 Metallpulver und Probe 132 4.3.4 Probenhalter 135 4.3.5 Probenstempel 135 4.3.6 Schraubenboden 136 4.3.7 Stahlronde 136 4.3.8 HARDOX‐Unterlage 137 5. Berechnung der Zustandsgleichungen für die Impedanzmethode mit Hilfe der Software MatLab 139 5.1 Randbedingungen 139 5.2 Tests der Möglichkeit der Verwendung der getroffenen Annahmen 142 5.2.1 Gültigkeit der linearen Up‐Us‐Relation anstelle quadratischer Gleichungen 141 5.2.2 Verwendung der gespiegelten Hugoniot anstelle der adiabatischen Entspannungskurve 144 5.3 Berechnung der Hugoniot-EoS für die Kollision der Flugplatte mit dem Probencontainer 145 5.4 Berechnung der Kenngrößen „Druck“ und „Dichte“ für das Metallpulver mit Hilfe der Rankine‐Hugoniot‐EoS 152 5.5 Überprüfung der mit MatLab berechneten Zustandsgrößen 156 5.6 Berechnung der Kenngröße „Schocktemperatur“ für Kupferpulver im festen Zustand mit Hilfe der Mie‐Grüneisen‐EoS 158 5.7 Erstellen des X‐t‐Diagramms sowie Berechnung der Kenngröße „Schockdauer“ mit Hilfe linearer Gleichungssysteme 162 6. Empirisch methodische Weiterentwicklungen der Synthesemethoden 169 6.1 Vermeidung von Mach-Effekten 169 6.2 Impedanzkorrektur der Probeneinheit 173 6.2.1 Zerstörung des Probencontainers infolge ungünstiger Impedanzverhältnisse 173 6.2.2 Die Impedanzfunktion als zeit- und ortsaufgelöster Bestandteil der Hugoniot‐EoS 175 6.2.3 Konsequenzen der orts‐ und zeitabhängigen Impedanz- funktion für die Materialauswahl der Probeneinheit 180 6.3 Die Rolle der adiabatischen Dekompression unter Einbeziehung zusätzlicher Volumina. 183 7. Anwendungen 197 7.1 Untersuchungen des Microjettings 197 7.2 Reflektionsmethode mit Impedanzkorrigierter Probeneinheit und gekapseltem Reflektor 207 7.2.1 Versuchsaufbau 207 7.2.2 Testergebnisse 209 7.2.3 Berechnung der Druck‐ und Temperaturbedingungen für die Reflektionsmethode mit Hilfe der Software MatLab 211 7.2.3.1 Berechnung des p=f(Up)-Diagramms 211 7.2.3.2 Berechnung der Temperatur sowie der Geschwindigkeiten Up und Us 215 7.3 Halidbasierte Schockwellenbeanspruchung fluidreicher Phasen 222 7.4 Synthese von rs-AlN sowie -Si3N4 222 7.5 Upscaling der impedanzkorrigierten Probeneinheit mit vollständiger Probenrückgewinnung 223 7.5.1 Versuchsaufbau 223 7.5.2 Ergebnisse 225 8. Schlussfolgerungen 229 9. Danksagung 234 Literaturverzeichnis 235

Ziel der Arbeit war die Synthese von ZnS, welches strukturell natürlichen Sphalerit imitieren und für die Untersuchung und Optimierung von biologischen Laugungsexperimenten genutzt werden soll. Zur Herstellung von chemisch reinem sowie mit den Wertelementen Indium, Kupfer und Eisen dotierten ZnS wurden vier verschiedene Synthesemethoden getestet: Ofentempern, chemische Gasphasentransportreaktion (CVT), feldunterstütztes Sintern (SPS) und die Hochdruck-Hochtemperatur-Synthese (HP/HT). Es folgte die Charakterisierung der synthetisierten Produkte hinsichtlich der Realstruktur und chemischen Reinheit mittels XANES, REM, XRD, EPMA und nasschemischer Verfahren. Abschließend wurden die Synthesemethoden nach ihrer Effizienz evaluiert. Das Ziel, defektfreies kubisches ZnS zu erzeugen, wurde nur mittels CVT und HP/HT erreicht. In dieser Arbeit konnte weiterhin gezeigt werden, dass der Einbau von Indium ohne gleichzeitige Aufnahme von Kupfer bis zu 1 Ma-% möglich ist.:Abbildungsverzeichnis VII Tabellenverzeichnis XI Abkürzungen, Akronyme und Symbole XII Einheiten XV 1 Einleitung 1 2 Forschungsstand zur Synthese von Zinksulfid 6 2.1 Kristallographie von ZnS . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 8 2.2 p-T -Phasendiagramm von ZnS . . . . . . . . . . . . . . . . . . . . . . . . . . . 12 3 Synthesematerial 15 3.1 Gefälltes ZnS . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 15 3.2 Dotierungsmaterialien . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 17 3.3 Recherche zu kommerziellen Metallsulfiden . . . . . . . . . . . . . . . . . . . . 18 4 Synthesemethoden 21 4.1 Ofentempern . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 22 4.2 FAST-SPS . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 23 4.3 CVT . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 24 4.4 HP/HT-Synthese . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 26 4.4.1 Toroid-Zelle . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 26 4.4.2 HP/HT-Experimentalaufbau und -ablauf . . . . . . . . . . . . . . . . . 27 4.4.3 HP/HT-Kalibrierung . . . . . . . . . . . . . . . . . . . . . . . . . . . . 32 5 Analysemethoden 42 5.1 ICP-MS & ICP-OES . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 43 5.2 XRD . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 44 5.3 UV-VIS . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 55 5.4 REM-EDX . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 55 5.5 EBSD . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 56 5.6 EPMA . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 57 5.7 XANES Spektroskopie . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 58 5.8 Ramanspektroskopie . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 61 5.9 Dichtebestimmung . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 62 5.10 BET-Messung . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 62 6 Ergebnisse 63 6.1 Charakterisierung industriell verfügbarer Materialien und natürlicher Proben . 63 6.1.1 Synthetische, industriell verfügbare Materialien . . . . . . . . . . . . . . 63 6.1.2 Referenzspektren für XANES-Analysen . . . . . . . . . . . . . . . . . . 65 6.2 Charakterisierung der Synthesematerialien . . . . . . . . . . . . . . . . . . . . 74 6.2.1 ZnS der Leuchtstoffwerke Breitungen GmbH (LWB) . . . . . . . . . . . 74 6.2.2 Dotierungsmaterialien In, Cu und Fe . . . . . . . . . . . . . . . . . . . . 77 6.3 Charakterisierung der synthetisierten Produkte . . . . . . . . . . . . . . . . . . 80 6.3.1 Einkristalle (CVT) . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 80 6.3.2 Polykristalline Produkte (Ofentempern, FAST-SPS und HP/HT) . . . . 112 6.4 Bestimmung des Stapelfehleranteils mittels Ramanspektroskopie? . . . . . . . . 152 7 Diskussion 155 7.1 Synthesematerialien und industriell verfügbare Materialien . . . . . . . . . . . 155 7.2 Syntheseprodukte . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 160 7.2.1 Syntheseprodukte: Einkristalle (CVT) . . . . . . . . . . . . . . . . . . . 160 7.2.2 Syntheseprodukte: Polykristalline Produkte (Ofentempern, FAST-SPS und HP/HT) . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 183 7.2.3 Vergleich der Syntheseprodukte: Einkristalle und Polykristalline Produkte 202 8 Laugungsexperimente: Zusammenfassung und Schlussfolgerung 213 9 Schlussfolgerung 220 10 Zusammenfassung 221 Literaturverzeichnis 225 Anhang A Ergebnispräsentation auf internationalen Fachtagungen 247 B Pulver vs. Kompaktprobe-Diffraktometrie 249 C ZnSdis.str-Datei 252 D Bestimmung der Bandlücke 254 E Messpunkte EPMA 256 F Einwaagen der Synthese 258 G Texturfaktoren der Röntgenbeugung X-Ray Diffraction (XRD)-Analyse 260

Trace component analysis in gasification processes are important part of elemental component balances in order to understand the fate of these participating compounds in the feedstock. Residual traces in the raw synthesis gas after quench could bring about the poisoning of catalysts and corrosion effects on plant facilities. The objective of this work is to investigate the effects of quenching operation on the trace components during test campaigns of the autothermal non-catalytic reforming of natural gas (Gas-POX) mode in the HP POX (high pressure partial oxidation) test plant. In order to achieve this, Aspen Plus simulation model of the quench chamber of the HP POX test plant was developed to re-calculate the quench chamber input amount of different trace compounds from their output amount measured during test points of the Gas-POX campaigns. Variation in quench water temperatures from 130 °C to 220 °C and pH value of quench water as well as the resulting variation in Henry´s and Dissociation constant of the traces (CO2, H2S, NH3 and HCN) changed the distribution of traces calculated in the quench water. The formation of traces of organic acid (formic acid and acetic acid) and traces of BTEX, PAHs and soot in the quench water effluent were discussed. The discrepancies between equilibrium constant and reaction quotient (non-equilibrium or real) for the formation of NH3 and HCN at the exit of the gasifier were discussed. The assessment of the results in this work should lead to the improvement in the understanding of trace components and concepts that could be employed to influence their formation and reduction.

Trace component analysis in gasification processes are important part of elemental component balances in order to understand the fate of these participating compounds in the feedstock. Residual traces in the raw synthesis gas after quench could bring about the poisoning of catalysts and corrosion effects on plant facilities. The objective of this work is to investigate the effects of quenching operation on the trace components during test campaigns of the autothermal non-catalytic reforming of natural gas (Gas-POX) mode in the HP POX (high pressure partial oxidation) test plant. In order to achieve this, Aspen Plus simulation model of the quench chamber of the HP POX test plant was developed to re-calculate the quench chamber input amount of different trace compounds from their output amount measured during test points of the Gas-POX campaigns. Variation in quench water temperatures from 130 °C to 220 °C and pH value of quench water as well as the resulting variation in Henry´s and Dissociation constant of the traces (CO2, H2S, NH3 and HCN) changed the distribution of traces calculated in the quench water. The formation of traces of organic acid (formic acid and acetic acid) and traces of BTEX, PAHs and soot in the quench water effluent were discussed. The discrepancies between equilibrium constant and reaction quotient (non-equilibrium or real) for the formation of NH3 and HCN at the exit of the gasifier were discussed. The assessment of the results in this work should lead to the improvement in the understanding of trace components and concepts that could be employed to influence their formation and reduction.:List of Figures vii List of Tables xii List of Abbreviations and Symbols xiii 1 Introduction 1 1.1 Background 1 1.2 Objective of the Work 4 1.3 Overview of the Work 5 2 Process and test conditions 6 2.1 HP POX test plant 6 2.2 Test campaign procedure 8 2.2.1 Gas-POX operating parameter range 8 2.2.2 Gas-POX experiments 9 2.2.3 Net reactions of partial oxidation 9 2.3 Gaseous feedstock characterization 11 2.3.1 Natural gas feedstock composition 11 2.4 Analytical methods for gaseous products 12 2.4.1 Hot gas sampling 12 2.4.2 Raw synthesis gas analysis after quench 13 2.5 Aqueous phase product analysis 14 2.5.1 Molecularly dissolved trace compounds and their ions trace analysis 14 2.5.2 Other trace analysis 15 2.6 Limit of accuracy in measurement systems 15 2.7 Summary 17 3 Simulation and methods 18 3.1 Test points calculation of the HP POX test campaign 18 3.1.1 Aspen Plus model for HP POX quench water system 19 3.2 Gas-POX 201 VP1 quench water system model simulation by Aspen Plus 23 3.2.1 Measured and calculated input parameters 23 3.2.2 Calculated sensitivity studies of species and their distribution for test point (VP1) 24 3.3 Used calculation tools related to the work 25 3.3.1 VBA in Excel 25 3.3.2 Python as interface between Aspen Plus and Microsoft Excel 26 3.3.3 Aspen Simulation Workbook 27 3.4 Summary 29 4 Trace components in quench water system 30 4.1 Physico-chemical parameters of quench water 31 4.1.1 Quench water pH adjustment 32 4.1.2 Henry constant 34 4.1.3 Dissociation constant 35 4.1.4 Organic acids in quench water 38 4.2 Carbon dioxide (CO2) 39 4.2.1 Results of sensitivity study: quench water temperature variation effects on CO2 41 4.2.2 Results of sensitivity study: quench water pH variation influence on CO2 42 4.3 Nitrogen compounds 43 4.3.1 Ammonia (NH3) 44 4.3.2 Results of sensitivity study: quench water temperature variation effects on NH3 46 4.3.3 Results of sensitivity study: quench water pH variation influence on NH3 47 4.3.4 Hydrogen Cyanide (HCN) 48 4.3.5 Results of sensitivity study: quench water temperature variation effects on HCN 50 4.3.6 Results of sensitivity study: quench water pH variation influence on HCN 50 4.4 Sulphur compounds: H2S 51 4.4.1 Results of sensitivity study: quench water temperature variation effects on H2S 53 4.4.2 Results of sensitivity study: quench water pH variation influence on H2S 54 4.5 Summary 55 5 Organic acids trace studies in quench water 57 5.1 Organic acids interaction with ammonia compounds in the quench water 57 5.2 Formic acid 62 5.2.1 Trace of formic acid in quench water 64 5.3 Acetic acid 67 5.3.1 Trace of acetic acid in quench water 69 5.4 Summary 72 6 Temperature approach studies for NH3 and HCN formation in gasifier 74 6.1 Nitrogen compounds: NH3 and HCN 74 6.2 Ammonia (NH3) formation in the gasifer 77 6.3 Hydrogen cyanide (HCN) formation in the gasifier 79 6.4 Discrepancies between back-calculated reaction quotients and equilibrium constants of the NH3 formation 81 6.4.1 Case 1: calculated equilibrium distribution between N2, NH3 and HCN 81 6.4.2 Case 2: calculated equilibrium distribution between NH3 and HCN 83 6.5 Summary 84 7 Traces of BTEX, PAHs and soot in quench water 86 7.1 Quench water behaviour 87 7.2 BTEX compounds 88 7.2.1 BTEX in quench water effluent 90 7.3 PAH compounds 93 7.3.1 PAHs in quench water effluent 95 7.4 Soot formation 99 7.4.1 Soots in quench water effluent 101 7.5 Summary 102 8 Summary and outlook 103 Bibliography 106 9 Appendix 135 List of Figures Figure 2.1: HP POX test plant main facility components and material flow courtesy of [Lurgi GmbH, 2008] 6 Figure 2.2: Simplified scheme of HP POX plant (including quench system) [Lurgi GmbH, 2008] 7 Figure 2.3: Overview of reactions of methane 10 Figure 3.1: Simplified scheme for HP POX quench water system 18 Figure 3.2: Aspen Plus flow diagrams of simulated HP POX quench water system 19 Figure 3.3: Integration of information and functions in VBA via Microsoft Excel to Aspen Plus model 25 Figure 3.4: Integration of information and functions in Python via Microsoft Excel to Aspen Plus model 26 Figure 3.5: ASW enables Excel users to rapidly run scenarios using the underlying rigorous models to analyze plant data, monitor performance, and make better decisions. 27 Figure 4.1: Vapour-liquid equilibria system of CO2, H2S, NH3, HCN and organic acids in the quench water and extended mechanisms according to [Kamps et al., 2001], [Alvaro et al., 2000], [Kuranov et al., 1996], [Xia et al., 1999] and [Edwards et al., 1978]. 30 Figure 4.2: HP POX quench water system with pH regulator for sensitivity studies 34 Figure 4.3: Henry´s constant for CO2, H2S, NH3 and HCN derived from [Edwards et al., 1978] for CO2, [Alvaro et al., 2000] for NH3, [Kamps et al., 2001] for H2S, and [Rumpf et al., 1992] for HCN 35 Figure 4.4: Dissociation constants for CO2, H2S, NH3, HCN and H2O derived from [Alvaro et al., 2000], [Kamps et al., 2001], and [Edwards et al., 1978] 37 Figure 4.5: The flow of CO2 in the quench water cycle (test point VP1). 40 Figure 4.6: Calculated quench water temperature variation and effects on CO2 distribution 42 Figure 4.7: Calculated influence of pH regulation and effects on CO2 distribution 43 Figure 4.8: The flow of NH3 in the quench water cycle (test point VP1). 46 Figure 4.9: Calculated quench water temperature variation and effects on NH3 distribution 47 Figure 4.10: Calculated influence of pH regulation and effects on NH3 distribution 48 Figure 4.11: The flow of HCN in the quench water cycle (test point VP1). 49 Figure 4.12: Calculated quench water temperature variation and effects on HCN distribution 50 Figure 4.13: Calculated influence of pH regulation and effects on HCN distribution 51 Figure 4.14: The flow of H2S in the quench water cycle (test point VP1) 53 Figure 4.15: Calculated quench water temperature variation and effects on H2S distribution 54 Figure 4.16: Calculated influence of pH regulation and effects on H2S distribution 55 Figure 5.1: Aspen Plus back-calculated (real) formic acid concentration, quench water temperature and the calculated equilibrium formic acid concentration against back-calculated (real) ammonia concentration for the 47 test points (using amongst others sampled HCOO- and NH4+ values according to Table 2.6). 59 Figure 5.2: Aspen plus back-calculated (real) formic acid concentration, back-calculated (real) ammonia concentration and the calculated equilibrium formic acid concentration against quench water temperature for the 47 test points (using amongst others sampled HCOO- and NH4+ values according to Table 2.6). 60 Figure 5.3: Aspen plus back-calculated (real) acetic acid concentration, quench water temperature and the calculated equilibrium acetic acid concentration against back-calculated (real) ammonia concentration for the 47 test points. 61 Figure 5.4: Aspen plus back-calculated (real) acetic acid concentration, back-calculated (real) ammonia concentration and the calculated equilibrium acetic acid concentration against quench water temperature for the 47 test points. 62 Figure 5.5: Concentration of formic acid (Aspen plus calculated m_eq and back-calculted m_real) formation in the quench and quench water temperature for the 47 test points. 64 Figure 5.6: Concentration of formic acid (Aspen plus calculated m_eq and back-calculted m_real) in the quench against quench water temperature for the 47 test points (as in Fig.5.2). 65 Figure 5.7: Comparison between formic acid equilibrium constant (Keq), reaction quotient (Kreal) and the quench water temperature for the 47 test points. 66 Figure 5.8: Comparison between formic acid equilibrium constant (Keq) and reaction quotient (Kreal) against quench water temperatures for the 47 test points. 67 Figure 5.9: Concentration of acetic acid (Aspen plus calculated m_eq and back-calculted m_real) in the quench and quench water temperature for the 47 test points. 69 Figure 5.10: Concentration of acetic acid (Aspen plus calculated m_eq and back-calculted m_real) in the quench against quench water temperature for the 47 test points (as in Fig.5.4). 70 Figure 5.11: Comparison between acetic acid equilibrium constant (Keq), reaction quotient (Kreal) and the quench water temperature for the 47 test points. 71 Figure 5.12: Comparison between acetic acid equilibrium constant (Keq) and reaction quotient (Kreal) against quench water temperatures for the 47 test points. 72 Figure 6.1: Mole fraction of gas compoents in the hot gas outlet out of gasifier against hot gas temperature for the 47 test points 76 Figure 6.2: Calculated reaction quotient (Q) and equlibrium constant (Keq) for NH3 against hot gas temperature for the 47 test points (see Fig. 9.10 in Appendix) 77 Figure 6.3: NH3 temperature approach against hot gas temperature for the 47 test points (see Fig. 9.11 in Appendix) 78 Figure 6.4: Calculated reaction quotient (Q) and equlibrium constant (Keq) for HCN against hot gas temperature for the 47 test points (see Fig. 9.13 in Appendix) 79 Figure 6.5: HCN temperature approach against hot gas temperature for the 47 test points (see Fig. 9.14 in Appendix) 80 Figure 6.6: Comparison between calculated real and equilibrium hot gas N2, NH3 and HCN mol fractions against their respective hot gas temperature (case 1). 82 Figure 6.7: Relations between back-calculated real and equilibrium hot gas N2, NH3 and HCN mol fractions (for chemical equilibrium according to equations (6.1) and (6.4)) against their respective hot gas temperature (see Case 1, Section 6.4.1, and Fig. 6.6) 82 Figure 6.8: Comparison between calculated real and equilibrium hot gas HCN mol fraction against their respective hot gas temperature (case 2). 83 Figure 6.9: Relations between back-calculated real and equilibrium hot gas HCN mol fractions, and change in NH3 mol fractions (for chemical equilibrium according to equation (6.4)), against their respective hot gas temperature (see. Case 2, Section 6.4.2 and Fig. 6.7) 84 Figure 6.10 Comparison between NH3 and HCN formation (mole fraction) calculated equilibrium constant (Keq) and calculated reaction quotient (Q), N2 consumption and hot gas temperatures for the 47 test points (case 1 and case 2). 85 Figure 7.1: HP POX test plant quench water system 88 Figure 7.2: Traces of BTEX measured in the Gas-POX 203 – 207 quench water effluent sample. 91 Figure 7.3: Individual component of BTEX measured in the Gas-POX 203 – 207 quench water effluent sample. 92 Figure 7.4: (a) Alkyl radical decomposition and (b) C1 and C2 hydrocarbons oxidation mechanism [Warnatz et al., 2000] 93 Figure 7.5: Recombination of C3H3 to form benzene 94 Figure 7.6: The Diels - Alder reaction for the formation of PAHs 95 Figure 7.7: Amount of PAHs that were detected in Gas-POX 203 – 207 test points quench water effluent samples. 97 Figure 7.8: Distribution of PAH compounds in Gas-POX 203 – 207 quench water effluent samples. 98 Figure 7.9: Some steps in soot formation [McEnally et al., 2006]. 99 Figure 7.10: Illustration of soot formation path in homogenous mixture [Bockhorn et al., 1994] 100 Figure 9.1: Aspen flow sheet set up for HP POX quench system GasPOX 201 VP1 (simplified and extension of Fig. 3.2, organic acids not taken into account). Tabulated values are given in Table 9.11. 135 Figure 9.2: Comparison between the Henry´s constant profiles: Aspen Plus (markers) and Literatures (solid lines) ([Edwards et al., 1978] for CO2, [Alvaro et al., 2000] for NH3, [Kamps et al., 2001] for H2S, and [Rumpf et al., 1992] for HCN as it can be seen in Fig. 4.3) 137 Figure 9.3: Henry´s constant profiles derived from literatures ([Edwards et al., 1978] for CO2, [Alvaro Pérez-Salado et al., 2000] for NH3, [Kamps et al., 2001] for H2S, and [Rumpf et al., 1992] for HCN as it can be seen in Fig. 4.3) 137 Figure 9.4: Comparison between the dissociation constant profiles: Aspen Plus (markers) and Literatures (solid or dashed lines) [Alvaro et al., 2000], [Kamps et al., 2001], and [Edwards et al., 1978] as in Fig.4.4. 138 Figure 9.5: Dissociation constant profiles derived from literatures [Kamps et al., 2001], and [Edwards et al., 1978] as in Fig.4.4. 138 Figure 9.6: Calculated pH values, temperature range and species 139 Figure 9.7: Aspen Plus flow sheet setup for organic acid compounds calculations (GasPOX 201 VP1, see also Table 9.12) 142 Figure 9.8: Aspen Plus flow sheet setup for nitrogen compounds calculations (GasPOX 201 VP1, see also Table 9.12, organic acids are taken into account in the aqueous streams of the quench system) 145 Figure 9.9: Yield of ammonia in gasifier (calculated real) and hot gas temperature against the 47 test points 146 Figure 9.10: Kreal or reaction quotient for ammonia formation in the gasifier against the 47 test points. 146 Figure 9.11: Temperature approach studies for ammonia and the 47 test points 147 Figure 9.12: Yield of HCN from the gasifier (calculated real and equilibrium) and hot gas temperature and the 47 test points 147 Figure 9.13: Comparison between equilibrium constant and reaction quotient for HCN and 47 test points 148 Figure 9.14: Temperature approach studies for HCN and the 47 test points 148 Figure 9.15: Comparison among equilibrium constants of reactions against temperature, T [°C] 149 Figure 9.16: Comparison among equilibrium constants of reactions against temperature, 1/T [1/K] 150 List of Tables Table 2.1: Outline of Gas-POX mode operating parameter range 8 Table 2.2: Outline of test runs operating mode and parameters of chosen test campaigns 9 Table 2.3: Natural gas feedstock compositions 12 Table 2.4: Product synthesis gas analysis method (hot gas before quench) [Brüggemann, 2010] 12 Table 2.5: Analysis methods for raw synthesis gas [Brüggemann, 2010] 13 Table 2.6: Analysis methods for aqueous phase products [Brüggemann, 2010] 14 Table 2.7: Relative accuracy for the measured value for temperature, pressure and flow of each feed and product stream [Meyer, 2007] and [Brüggemann, 2010] 17 Table 3.1: Description of blocks used in Aspen Plus simulation. 20 Table 3.2: HP POX test plant quench water cycle parameters Gas-POX 201 VP1* 23 Table 3.3: pH regulator parameters 24 Table 4.1: Organic acids distribution in streams for VP1 based on calculation from Aspen Plus. 38 Table 4.2: The distribution of CO2 and its ions in all the streams 40 Table 4.3: The distribution of NH3 and its ions in all the streams 45 Table 4.4: The distribution of HCN and its ions in all the streams 49 Table 4.5: The distribution of H2S and its ions in all the streams 52 Table 7.1: Relative sooting tendency [Tesner et al., 2010] 101 Table 9.1: Natural gas feed analysis method [Brüggemann, 2010] 135 Table 9.2: pH scale with examples of solution [NALCO 2008] 136 Table 9.3: Gas-POX test campaigns and with designated serial numbers 140 Table 9.4: Summary of correlation coefficient (r) from Figures in Chapter 5 144 Table 9.5: Comparison among reactions temperatures and heat of reactions 149 Table 9.6: Content of BTEX compounds in Gas-POX quench water samples 151 Table 9.7: BTEX in quench water effluent samples results 152 Table 9.8: Content of PAH compounds in Gas-POX quench water samples 157 Table 9.9: PAHs in quench water effluent samples results 160 Table 9.10: Soot in quench water effluent samples results 169 Table 9.11: Aspen Plus flow sheet setup stream details (GasPOX 201 VP1, according to Fig.3.2 and Fig.9.1, organic acids not taken into account) 170 Table 9.12: Aspen Plus flow sheet setup for organic acid and nitrogen compounds calculations for GasPOX 201 VP1 (according to Figures 9.7 and 9.8, organic acids are taken into account) 174