The purpose of this essay is to determine how the two former prime-minister of Sweden Olof Palme and Stefan Löfven speak of economic equality in their proclamations of government. Furthermore the essay investigates if there has been a shift in socialist ideology between the two prime-ministers from reformist socialism towards the third way. To investigate this the essay analyzed proclamations of government using ideology analysis to find how they spoke of economic equality. Ideal-types were also used to find if parts of their proclamations of government were closer to reformist socialism or third way socialism. In short the essay concluded that both prime-ministers spoke extensively of economic equality, Palme more so than Löfven, furthermore I found that Löfven cloud be considered closer to third way socialism in the area of economic equality. This study is an addition to the field of study on economic equality and the shift towards third way socialism among social democratic parties in Europe.

No description available.

This thesis is concerned with motion planning for the classical two-phase Stefan problem in level set formulation. The interface separating the fluid phases from the solid phases is represented as the zero level set of a continuous function whose evolution is described by the level set equation. Heat conduction in the two phases is modeled by the heat equation. A quadratic tracking-type cost functional that incorporates temperature tracking terms and a control cost term that expresses the desire to have the interface follow a prescribed trajectory by adjusting the heat flux through part of the boundary of the computational domain. The formal Lagrange approach is used to establish a first-order optimality system by applying shape calculus tools. For the numerical solution, the level set equation and its adjoint are discretized in space by discontinuous Galerkin methods that are combined with suitable explicit Runge-Kutta time stepping schemes, while the temperature and its adjoint are approximated in space by the extended finite element method (which accounts for the weak discontinuity of the temperature by a dynamic local modification of the underlying finite element spaces) combined with the implicit Euler method for the temporal discretization. The curvature of the interface which arises in the adjoint system is discretized by a finite element method as well. The projected gradient method, and, in the absence of control constraints, the limited memory BFGS method are used to solve the arising optimization problems. Several numerical examples highlight the potential of the proposed optimal control approach. In particular, they show that it inherits the geometric flexibility of the level set method. Thus, in addition to unidirectional solidification, closed interfaces and changes of topology can be tracked. Finally, the Moreau-Yosida regularization is applied to transform a state constraint on the position of the interface into a penalty term that is added to the cost functional. The optimality conditions for this penalized optimal control problem and its numerical solution are discussed. An example confirms the efficacy of the state constraint. / Die vorliegende Arbeit beschäftigt sich mit einem Optimalsteuerungsproblem für das klassische Stefan-Problem in zwei Phasen. Die Phasengrenze wird als Niveaulinie einer stetigen Funktion modelliert, was die Lösung der so genannten Level-Set-Gleichung erfordert. Durch Anpassen des Wärmeflusses am Rand des betrachteten Gebiets soll ein gewünschter Verlauf der Phasengrenze angesteuert werden. Zusammen mit dem Wunsch, ein vorgegebenes Temperaturprofil zu approximieren, wird dieses Ziel in einem quadratischen Zielfunktional formuliert. Die notwendigen Optimalitätsbedingungen erster Ordnung werden formal mit Hilfe der entsprechenden Lagrange-Funktion und unter Benutzung von Techniken aus der Formoptimierung hergeleitet. Für die numerische Lösung müssen die auftretenden partiellen Differentialgleichungen diskretisiert werden. Dies geschieht im Falle der Level-Set-Gleichung und ihrer Adjungierten auf Basis von unstetigen Galerkin-Verfahren und expliziten Runge-Kutta-Methoden. Die Wärmeleitungsgleichung und die entsprechende Gleichung im adjungierten System werden mit einer erweiterten Finite-Elemente-Methode im Ort sowie dem impliziten Euler-Verfahren in der Zeit diskretisiert. Dieser Zugang umgeht die aufwändige Adaption des Gitters, die normalerweise bei der FE-Diskretisierung von Phasenübergangsproblemen unvermeidbar ist. Auch die Krümmung der Phasengrenze wird numerisch mit Hilfe der Methode der finiten Elemente angenähert. Zur Lösung der auftretenden Optimierungsprobleme werden ein Gradienten-Projektionsverfahren und, im Fall dass keine Kontrollschranken vorliegen, die BFGS-Methode mit beschränktem Speicherbedarf eingesetzt. Numerische Beispiele beleuchten die Stärken des vorgeschlagenen Zugangs. Es stellt sich insbesondere heraus, dass sich die geometrische Flexibilität der Level-Set-Methode auf den vorgeschlagenen Zugang zur optimalen Steuerung vererbt. Zusätzlich zur gerichteten Bewegung einer flachen Phasengrenze können somit auch geschlossene Phasengrenzen sowie topologische Veränderungen angesteuert werden. Exemplarisch, und zwar an Hand einer Beschränkung an die Lage der Phasengrenze, wird auch noch die Behandlung von Zustandsbeschränkungen mittels der Moreau-Yosida-Regularisierung diskutiert. Ein numerisches Beispiel demonstriert die Wirkung der Zustandsbeschränkung.

This thesis is concerned with motion planning for the classical two-phase Stefan problem in level set formulation. The interface separating the fluid phases from the solid phases is represented as the zero level set of a continuous function whose evolution is described by the level set equation. Heat conduction in the two phases is modeled by the heat equation. A quadratic tracking-type cost functional that incorporates temperature tracking terms and a control cost term that expresses the desire to have the interface follow a prescribed trajectory by adjusting the heat flux through part of the boundary of the computational domain. The formal Lagrange approach is used to establish a first-order optimality system by applying shape calculus tools. For the numerical solution, the level set equation and its adjoint are discretized in space by discontinuous Galerkin methods that are combined with suitable explicit Runge-Kutta time stepping schemes, while the temperature and its adjoint are approximated in space by the extended finite element method (which accounts for the weak discontinuity of the temperature by a dynamic local modification of the underlying finite element spaces) combined with the implicit Euler method for the temporal discretization. The curvature of the interface which arises in the adjoint system is discretized by a finite element method as well. The projected gradient method, and, in the absence of control constraints, the limited memory BFGS method are used to solve the arising optimization problems. Several numerical examples highlight the potential of the proposed optimal control approach. In particular, they show that it inherits the geometric flexibility of the level set method. Thus, in addition to unidirectional solidification, closed interfaces and changes of topology can be tracked. Finally, the Moreau-Yosida regularization is applied to transform a state constraint on the position of the interface into a penalty term that is added to the cost functional. The optimality conditions for this penalized optimal control problem and its numerical solution are discussed. An example confirms the efficacy of the state constraint. / Die vorliegende Arbeit beschäftigt sich mit einem Optimalsteuerungsproblem für das klassische Stefan-Problem in zwei Phasen. Die Phasengrenze wird als Niveaulinie einer stetigen Funktion modelliert, was die Lösung der so genannten Level-Set-Gleichung erfordert. Durch Anpassen des Wärmeflusses am Rand des betrachteten Gebiets soll ein gewünschter Verlauf der Phasengrenze angesteuert werden. Zusammen mit dem Wunsch, ein vorgegebenes Temperaturprofil zu approximieren, wird dieses Ziel in einem quadratischen Zielfunktional formuliert. Die notwendigen Optimalitätsbedingungen erster Ordnung werden formal mit Hilfe der entsprechenden Lagrange-Funktion und unter Benutzung von Techniken aus der Formoptimierung hergeleitet. Für die numerische Lösung müssen die auftretenden partiellen Differentialgleichungen diskretisiert werden. Dies geschieht im Falle der Level-Set-Gleichung und ihrer Adjungierten auf Basis von unstetigen Galerkin-Verfahren und expliziten Runge-Kutta-Methoden. Die Wärmeleitungsgleichung und die entsprechende Gleichung im adjungierten System werden mit einer erweiterten Finite-Elemente-Methode im Ort sowie dem impliziten Euler-Verfahren in der Zeit diskretisiert. Dieser Zugang umgeht die aufwändige Adaption des Gitters, die normalerweise bei der FE-Diskretisierung von Phasenübergangsproblemen unvermeidbar ist. Auch die Krümmung der Phasengrenze wird numerisch mit Hilfe der Methode der finiten Elemente angenähert. Zur Lösung der auftretenden Optimierungsprobleme werden ein Gradienten-Projektionsverfahren und, im Fall dass keine Kontrollschranken vorliegen, die BFGS-Methode mit beschränktem Speicherbedarf eingesetzt. Numerische Beispiele beleuchten die Stärken des vorgeschlagenen Zugangs. Es stellt sich insbesondere heraus, dass sich die geometrische Flexibilität der Level-Set-Methode auf den vorgeschlagenen Zugang zur optimalen Steuerung vererbt. Zusätzlich zur gerichteten Bewegung einer flachen Phasengrenze können somit auch geschlossene Phasengrenzen sowie topologische Veränderungen angesteuert werden. Exemplarisch, und zwar an Hand einer Beschränkung an die Lage der Phasengrenze, wird auch noch die Behandlung von Zustandsbeschränkungen mittels der Moreau-Yosida-Regularisierung diskutiert. Ein numerisches Beispiel demonstriert die Wirkung der Zustandsbeschränkung.

The design and optimization of entrained flow gasifiers is conducted more and more via computational fluid dynamics (CFD). A detailed resolution of single coal particles within such simulations is nowadays not possible due to computational limitations. Therefore the coal particle conversion is often represented by simple 0-D models. For an optimization of such 0-D models a precise understanding of the physical processes at the boundary layer and within the particle is necessary. In real gasifiers the particles experience Reynolds numbers up to 10000. However in the literature the conversion of coal particles is mainly regarded under quiescent conditions. Therefore an analysis of the conversion of single particles is needed. Thereto the computational fluid dynamics can be used. For the detailed analysis of single reacting particles under flow conditions a CFD model is presented. Practice-oriented parameters as well as features of the CFD model result from CFD simulations of a Siemens 200MWentrained flow gasifier. The CFD model is validated against an analytical model as well as two experimental data-sets taken from the literature. In all cases good agreement between the CFD and the analytics/experiments is shown. The numerical model is used to study single moving solid particles under combustion conditions. The analyzed parameters are namely the Reynolds number, the ambient temperature, the particle size, the operating pressure, the particle shape, the coal type and the composition of the gas. It is shown that for a wide range of the analyzed parameter range no complete flame exists around moving particles. This is in contrast to observations made by other authors for particles in quiescent atmospheres. For high operating pressures, low Reynolds numbers, large particle diameters and high ambient temperatures a flame exists in the wake of the particle. The impact of such a flame on the conversion of the particle is low. For high steam concentrations in the gas a flame appears, which interacts with the particle and influences its conversion. Furthermore the impact of the Stefan-flow on the boundary layer of the particle is studied. It is demonstrated that the Stefan-flow can reduce the drag coefficient and the Nusselt number for several orders of magnitude. On basis of the CFD results two new correlations are presented for the drag coefficient and the Nusselt number. The comparison between the correlations and the CFD shows a significant improvement of the new correlations in comparison to archived correlations. The CFD-model is further used to study moving single porous particles under gasifying conditions. Therefore a 2-D axis-symmetric system of non-touching tori as well as a complex 3-D geometry based on the an inverted settlement of monodisperse spheres is utilized. With these geometries the influence of the Reynolds number, the ambient temperature, the porosity, the intrinsic surface and the size of the radiating surface is analyzed. The studies show, that the influence of the flow on the particle conversion is moderate. In particular the impact of the flow on the intrinsic transport and conversion processes is mainly negligible. The size of the radiating surface has a similar impact on the conversion as the flow in the regarded parameter range. On basis of the CFD calculations two 0-D models for the combustion and gasification of moving particles are presented. These models can reproduce the results predicted by the CFD sufficiently for a wide parameter range.

Originally presented as the author's Thesis (doctoral--Ludwig-Maximilians-Universität, München, 2006). / Includes bibliographical references (p. 185-204).

Originally presented as the author's Thesis (doctoral--Ludwig-Maximilians-Universität, München, 2006). / Includes bibliographical references (p. 185-204).

The design and optimization of entrained flow gasifiers is conducted more and more via computational fluid dynamics (CFD). A detailed resolution of single coal particles within such simulations is nowadays not possible due to computational limitations. Therefore the coal particle conversion is often represented by simple 0-D models. For an optimization of such 0-D models a precise understanding of the physical processes at the boundary layer and within the particle is necessary. In real gasifiers the particles experience Reynolds numbers up to 10000. However in the literature the conversion of coal particles is mainly regarded under quiescent conditions. Therefore an analysis of the conversion of single particles is needed. Thereto the computational fluid dynamics can be used. For the detailed analysis of single reacting particles under flow conditions a CFD model is presented. Practice-oriented parameters as well as features of the CFD model result from CFD simulations of a Siemens 200MWentrained flow gasifier. The CFD model is validated against an analytical model as well as two experimental data-sets taken from the literature. In all cases good agreement between the CFD and the analytics/experiments is shown. The numerical model is used to study single moving solid particles under combustion conditions. The analyzed parameters are namely the Reynolds number, the ambient temperature, the particle size, the operating pressure, the particle shape, the coal type and the composition of the gas. It is shown that for a wide range of the analyzed parameter range no complete flame exists around moving particles. This is in contrast to observations made by other authors for particles in quiescent atmospheres. For high operating pressures, low Reynolds numbers, large particle diameters and high ambient temperatures a flame exists in the wake of the particle. The impact of such a flame on the conversion of the particle is low. For high steam concentrations in the gas a flame appears, which interacts with the particle and influences its conversion. Furthermore the impact of the Stefan-flow on the boundary layer of the particle is studied. It is demonstrated that the Stefan-flow can reduce the drag coefficient and the Nusselt number for several orders of magnitude. On basis of the CFD results two new correlations are presented for the drag coefficient and the Nusselt number. The comparison between the correlations and the CFD shows a significant improvement of the new correlations in comparison to archived correlations. The CFD-model is further used to study moving single porous particles under gasifying conditions. Therefore a 2-D axis-symmetric system of non-touching tori as well as a complex 3-D geometry based on the an inverted settlement of monodisperse spheres is utilized. With these geometries the influence of the Reynolds number, the ambient temperature, the porosity, the intrinsic surface and the size of the radiating surface is analyzed. The studies show, that the influence of the flow on the particle conversion is moderate. In particular the impact of the flow on the intrinsic transport and conversion processes is mainly negligible. The size of the radiating surface has a similar impact on the conversion as the flow in the regarded parameter range. On basis of the CFD calculations two 0-D models for the combustion and gasification of moving particles are presented. These models can reproduce the results predicted by the CFD sufficiently for a wide parameter range.:List of Figures . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . IX List of Tables . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .XIII Nomenclature . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . XV Abstract . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . XIX 1 Introduction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .1 1.1 State of the Art in Carbon Conversion Modeling . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4 1.1.1 Combustion of Solid Particles . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 4 1.1.2 Gasification of Porous Particles . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 6 1.2 Classification of the Present Work . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .7 1.3 Overview of the Work . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .7 2 Basic Theory and Model Formulation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 9 2.1 Geometry and Length Scales of Coal Particles . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .9 2.2 Conditions in a Siemens Like 200 MW Entrained Flow Gasifier . . . . . . . . . . . . . . . . . . . . 11 2.2.1 Velocity Field . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .12 2.2.2 Temperature Distribution . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 16 2.2.3 Particle Volume Fraction . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .19 2.3 Time Scales of the Physical Processes . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 20 2.4 Basic Assumptions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .21 2.5 Conservation Equations . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 22 2.6 Gas Properties . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .26 2.7 Boundary Conditions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 29 2.8 Numerics and Solution Strategy . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .30 2.9 Mesh and Domain . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .31 3 CFD-based Oxidation Modeling of a Non-Porous Carbon Particle . . . . . . . . . . . . . . . . . . . . .37 3.1 Chemical Reaction System for Combustion . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .37 3.1.1 Heterogeneous Reactions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .37 3.1.2 Homogeneous Reactions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .40 3.1.3 Comparison of the Semi-Global vs. Reduced Reaction Mechanisms for the Gas Phase . .41 3.2 Validation . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .43 3.2.1 Validation Against an Analytical Solution of the Two-Film Model . . . . . . . . . . . . . . . . . .43 3.2.2 Validation Against Experiments I . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 45 3.2.3 Validation Against Experiments II . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .49 3.3 Influence of Ambient Temperature and Reynolds Number . . . . . . . . . . . . . . . . . . . . . . . .51 3.4 Influence of Heterogeneous Kinetics . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 59 3.5 Influence of Atmosphere . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .61 3.6 Influence of Operating Pressure . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .66 3.7 Influence of Particle Diameter . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .70 3.8 The influence of Particle Shape . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 73 3.9 Impact of Stefan Flow on the Boundary Layer . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 80 3.9.1 Impact of Stefan Flow on the Drag Coefficient . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .83 3.9.2 Impact of Stefan Flow on the Nusselt and Sherwood Number . . . . . . . . . . . . . . . . . . . .85 3.10 Single-Film Sub-Model vs. CFD . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 90 3.11 Summary . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 96 4 CFD-based Numerical Modeling of Partial Oxidation of a Porous Carbon Particle . . . . . . . . . .99 4.1 Chemical Reaction System for Gasification . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 100 4.1.1 Heterogeneous Chemistry . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .100 4.1.2 Homogeneous Chemistry . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 101 4.2 Two-Dimensional Simulations . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 106 4.2.1 Geometry . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 106 4.2.2 Influence of Reynolds Number and Ambient Temperature . . . . . . . . . . . . . . . . . . . . . .109 4.2.3 Influence of Porosity and Internal Surface . . . . . . . .. . . . . . . . . . . . . . . . . . . . . . . . . 120 4.3 Comparative Three-Dimensional Simulations . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 126 4.3.1 Geometry . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .126 4.3.2 Results of the 3-D Calculations . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 127 4.4 Extended Sub-Model for Gasification . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .133 4.5 Summary . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .138 5 Conclusions . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .. . . . . . . . .141 5.1 Summary of This Work . . . . . . . . . . . . . . . . . . . . . . . . . .. . . . . . . . . . . . . . . . . . . . . . .141 5.2 Recommendations for Future Works . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 143 Bibliography . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .145 6 Appendix . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 157 6.1 Appendix I: Properties . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 157 6.2 Appendix II: Two-Film Model . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 158 6.3 Appendix III: Sub-Model for the Combustion of Solid Particles . . . . . . . . . . . . . . . . . . . . 160 6.4 Appendix IV: Sub-Model for the Gasification of Porous Particles . . . . . . . . . . . . . . . . . . . 161

En förutsägbar centralbank är en viktig del i teorin för ett väl fungerande inflationsmål med stabil prisstegringstakt på önskvärd nivå. Förutsägbarheten ämnar att styra marknadsagenternas förväntningar i linje med målet sådant att löner och priser sätts efter detta. Eftersom en högre förutsägbarhet delvis är synonymt med hur en centralbank inkorporerar systematik vad gäller förhållningssätt till förändringar i marknadsfaktorer torde därför också den förda räntepolitiken vara möjlig att till viss grad beskriva med en reaktionsfunktion. I den här studien testas de tre riksbankscheferna, Urban Bäckström, Lars Heikensten och Stefan Ingves förda räntepolitik mot ett antal variabler relevanta mot den teoretiska bakgrunden. Resultaten visar hur räntepolitiken förefaller ha blivit mer systematisk efter Urban Bäckströms tid som riksbankschef och hur systematiken verkar förändrats under Stefan Ingves tid. Riksbanken frångick marknadsförväntningar under finanskrisens ned- och uppgång och grundade beslut efter deras egen data i större utsträckning. Från 2014 förefaller Riksbanken tvärtom föra en politik i linje med marknadens förväntningar. Sammanfattningsvis kan Riksbanken idag beskrivas som mer ödmjuk om sin egen förmåga och hur denna för en politik därefter. Studien ger en inblick i vad som föranlett en förändrad reaktionsfunktion, och således också Riksbankens resonemang till en viss grad.

The inadequacy of Fick’s law to incorporate causality can be overcome by replacing it with the Green–Naghdi type II (GNII) flux relation. Combining the GNII assumption and conservation of mass leads to [see document for equation] where r (x, t) is the density function, S(p) is a source term and c¥ is a positive constant which carries (SI) units of m/sec. A general source term given by [see document for equation] is proposed. Here, the constants y and ps are the rate coefficient and saturation density respectively. The travelling wave solutions and numerical analysis of four special cases of equation (2), namely: Pearl-Verhulst Growth law, Zel’dovich Law, Newmann Law and Stefan- Boltzmann Law are investigated. For both analysis, results are compared with the available literature and extended for other cases. The numerical analysis is carried out by imposing well-studied Initial Boundary Value Problem and implementing a built-in method in the software package Mathematica 9. For Pearl-Verhulst source type, the results are compared to those found in literature [1]. Confirming the validity of built-in method for Pearl-Verhulst law, the generic built-in method is extended to study the transient signal response for similar initial boundary value problems when the source terms are Zel’dovich law, Newmann law and Stefan-Boltzmann law.