L’objectif de la thèse est de concevoir un design le plus optimisé possible d’une centrale à charbon pulvérisée fonctionnant en oxy-combustion. Une telle centrale intègre un système de production d’oxygène (ASU), une chaudière, un cycle électrogène, des équipements de dépollution ainsi qu’un système de purification et de compression du CO2 (CPU). Ainsi, dans un premier temps, la thèse portera sur la compréhension, l’analyse et la modélisation des différents procédés qui composent la chaîne d’une centrale fonctionnant en oxy-combustion. Ensuite, les performances et la configuration de la centrale seront optimisées de façon à réduire la destruction d’exergie tout s’assurant de la compétitivité économique de la solution ainsi obtenue. A l’issue de cette thèse, les origines des pertes exergétiques du système étudié et les schémas d’intégration permettant de maximiser les gains énergétique à l’échelle de la centrale seront identifiées. De plus, les stratégies de dépollution des fumées les plus adaptées seront définies et les nouveaux procédés intégrés seront évalués à la fois d’un point de vue technico-économiques et flexibilité. / The objective of the thesis is the conception of an optimized oxy-fired pulverized-coal power plant. Such a power plant is constituted of an oxygen production system (ASU), a boiler, power cycle, depollution equipments and a CO2 purification and compression system (CPU). After a first step consists in understanding, analyzing and modeling the different processes composing the oxy-combustion system; the work will focus on the optimization of the performances and the configuration of the power plant by minimizing exergy destructions while ensuring economic competitiveness of the obtained solution. At the end of the thesis, the origins of the exergetic losses in the system as well as the thermal integration scheme allowing the maximization of the energetic gains at power plant level will be identified. Additionally, the most adapted flue gas depollution strategies will be defined and the new integrated process schemes will be evaluated on both a techno-economic and flexibility basis.

La conception des procédés industriels doit s'adapter à la raréfaction des ressources naturelles à bas prix et au durcissement des réglementations visant à limiter leur impact environnemental. Ainsi, pour améliorer leur rentabilité économique et leur soutenabilité, leurs effluents doivent être considérés comme des ressources potentielles de matière et d'énergie qui peuvent être valorisées localement ou à un plus grande échelle en les partageant avec d'autres industries voisines en formant un écoparc industriel.Cette thèse présente une nouvelle approche systémique et systématique pour concevoir des réseaux de valorisation d'énergie et de matière optimisés simultanément. Trois modèles linéaires de complexité croissante ont été développés pour concevoir ces réseaux à l'échelle locale. Le premier modèle (M1) détermine la consommation minimale nécessaire de ressources fraîches. Le second modèle (M2) introduit une nouvelle superstructure permettant l'optimisation simultanée des besoins énergétiques et matière pour atteindre le minimum de coûts de fonctionnement. Le troisième modèle (M3) conçoit les réseaux optimaux d'allocation de matière et d'échangeurs de chaleur simultanément. Sa fonction objective est le coût total annualisé incluant les coûts d'investissement et de fonctionnement.L'utilisation des unités de régénération est rendu possible dans la structure des trois modèles précédents. Tous les types d'unités peuvent être représentés par un modèle simple avec des paramètres génériques utilisant des objets déjà définis dans la formulation du modèle M3.Finalement, l'application du modèle M3 est étendue à la conception d'écoparcs industriels grâce à de nouvelles notions (sites, clusters, réseaux intermédiaires de matière et de chaleur), obtenant ainsi un nouveau modèle M4. Ce modèle inclut dans sa fonction objective les coûts d'investissements des réseaux liés à leur topologie.Des cas d'études issus de la littérature sont utilisés pour valider la pertinence et les performances des modèles présentés. / The design of industrial processes needs to be adapted as cheap natural resources are scarcer and environmental standards are more stringent to limit their environmental footprints. In order to improve their cost-effectiveness as well as their sustainability, industrial effluents must considered as potential heat and mass resources whether they are recycled locally or at a larger scale by sharing them with other industrial companies; thus forming an eco-industrial park (EIP).This thesis presents a new systemic and systematic approach to design optimal mass allocation and heat exchanger networks simultaneously. Three linear models of incremental complexity have been developed to design optimal recovery networks at a local scale. The first linear model (M1) looks for the necessary minimum fresh resource consumption. The second linear model (M2) presents a new superstructure that allows optimizing mass and heat requirements simultaneously, targeting the minimum annual operating costs. The third linear model (M3) allows designing optimal mass allocation and heat exchanger networks simultaneously. Its objective function is the total annualized cost considering operating and capital costs.The opportunity to use regeneration units is added to the structure of the three previous models. Any type of these units can be represented by a simple model with the generic parameters based on objects already existing in the previous models formulations.Finally, a M3 model applicability is extended to the design of collaborative eco-industrial parks with additional concepts (sites, clusters, indirect heat and mass networks) to obtain a new M4 model. In this model, the capital costs related to the topology of the networks are taken into account in the objective function.The relevance and performances of the proposed models are validated with several case studies taken from the literature.

Zur Reduzierung von Treibhausgasemissionen und Energiekosten in der Industrie kann die Steigerung der Energieeffizienz durch Nutzung der verfügbaren Abwärme einen wichtigen Beitrag leisten. Mit den Methoden der Wärmeintegration kann das Abwärmepotenzial quantifiziert und systematisch Maßnahmen zur Nutzung von Abwärme identifiziert werden. Durch die mathematische Optimierung des Wärmetransports von Wärmequellen hin zu Wärmesenken kann ein Wärmeübertrager Netzwerk gebildet werden. Hierbei können je nach Formulierung der Zielfunktion des Optimierungsproblems der benötigte Energiebedarf, die Kosten oder Treibhausgasemissionen minimiert werden. In dieser Arbeit wird ein Ansatz für mehrperiodische Optimierungsprobleme weiterentwickelt und um die Einbindung von sensiblen und latenten thermischen Energiespeichern erweitert. Die Berücksichtigung des Phasenwechsels erfolgt mit Hilfe einer intervallweise linearen Funktion der Speichertemperatur. Durch Einführen von Binärvariablen erfolgt eine Berücksichtigung des jeweils relevanten Intervalls. Darüber hinaus wird eine Methode zur Berücksichtigung von Wärmeverlusten der Rohrleitungen vorgestellt. Die entwickelten Methoden werden in einem Fallbeispiel aus der Textilindustrie angewendet und im Rahmen von Sensitivitätsanalysen ausgewählte Einflussfaktoren untersucht. / Increasing the energy efficiency by using available waste heat can make an important contribution to reducing greenhouse gas emissions and energy costs in the industry. Heat integration methods can be used to quantify the waste heat potential and systematically identify measures for waste heat utilization. By mathematically optimizing the heat transport from heat sources to heat sinks, a heat exchanger network can be designed. Depending on the formulation of the objective function of the optimization problem, the required energy demand, costs or greenhouse gas emissions can be minimized. In this work, an approach for multiperiod optimization problems is further developed and extended to include sensible and latent thermal energy storage. The phase change is considered by an interval linear function of the storage temperature. By introducing binary variables, the relevant interval is taken into account. Furthermore, a method for including heat losses of pipelines is presented. The developed methods are applied in a case study from the textile industry and selected influencing factors are investigated within the scope of sensitivity analyses.

Catalytic hydrotreating (HDT) is a mature process technology practiced in the petroleum refining industries to treat oil fractions for the removal of impurities (such as sulfur, nitrogen, metals, asphaltene). Hydrotreating of whole crude oil is a new technology and is regarded as one of the more difficult tasks that have not been reported widely in the literature. In order to obtain useful models for the HDT process that can be confidently applied to reactor design, operation and control, the accurate estimation of kinetic parameters of the relevant reaction scheme are required. This thesis aims to develop a crude oil hydrotreating process (based on hydrotreating of whole crude oil followed by distillation) with high efficiency, selectivity and minimum energy consumption via pilot plant experiments, mathematical modelling and optimization. To estimate the kinetic parameters and to validate the kinetic models under different operating conditions, a set of experiments were carried out in a continuous flow isothermal trickle bed reactor using crude oil as a feedstock and commercial cobaltmolybdenum on alumina (Co-Mo/¿-Al2O3) as a catalyst. The reactor temperature was varied from 335°C to 400°C, the hydrogen pressure from 4 to10 MPa and the liquid hourly space velocity (LHSV) from 0.5 to 1.5 hr-1, keeping constant hydrogen to oil ratio (H2/Oil) at 250 L/L. The main hydrotreating reactions were hydrodesulfurization (HDS), hydrodenitrogenation (HDN), hydrodeasphaltenization (HDAs) and hydrodemetallization (HDM) that includes hydrodevanadization (HDV) and hydrodenickelation (HDNi). An optimization technique is used to evaluate the best kinetic models of a trickle-bed reactor (TBR) process utilized for HDS, HDAs, HDN, HDV and HDNi of crude oil based on pilot plant experiments. The minimization of the sum of the squared errors (SSE) between the experimental and estimated concentrations of sulfur (S), nitrogen (N), asphaltene (Asph), vanadium (V) and nickel (Ni) compounds in the products, is used as an objective function in the optimization problem using two approaches (linear (LN) and non-linear (NLN) regression). The growing demand for high-quality middle distillates is increasing worldwide whereas the demand for low-value oil products, such as heavy oils and residues, is decreasing. Thus, maximizing the production of more liquid distillates of very high quality is of immediate interest to refiners. At the same time, environmental legislation has led to more strict specifications of petroleum derivatives. Crude oil hydrotreatment enhances the productivity of distillate fractions due to chemical reactions. The hydrotreated crude oil was distilled into the following fractions (using distillation pilot plant unit): light naphtha (L.N), heavy naphtha (H.N), heavy kerosene (H.K), light gas oil (L.G.O) and reduced crude residue (R.C.R) in order to compare the yield of these fractions produced by distillation after the HDT process with those produced by conventional methods (i.e. HDT of each fraction separately after the distillation). The yield of middle distillate showed greater yield compared to the middle distillate produced by conventional methods in addition to improve the properties of R.C.R. Kinetic models that enhance oil distillates productivity are also proposed based on the experimental data obtained in a pilot plant at different operation conditions using the discrete kinetic lumping approach. The kinetic models of crude oil hydrotreating are assumed to include five lumps: gases (G), naphtha (N), heavy kerosene (H.K), light gas oil (L.G.O) and reduced crude residue (R.C.R). For all experiments, the sum of the squared errors (SSE) between the experimental product compositions and predicted values of compositions is minimized using optimization technique. The kinetic models developed are then used to describe and analyse the behaviour of an industrial trickle bed reactor (TBR) used for crude oil hydrotreating with the optimal quench system based on experiments in order to evaluate the viability of large-scale processing of crude oil hydrotreating. The optimal distribution of the catalyst bed (in terms of optimal reactor length to diameter) with the best quench position and quench rate are investigated, based upon the total annual cost. The energy consumption is very important for reducing environmental impact and maximizing the profitability of operation. Since high temperatures are employed in hydrotreating (HDT) processes, hot effluents can be used to heat other cold process streams. It is noticed that the energy consumption and recovery issues may be ignored for pilot plant experiments while these energies could not be ignored for large scale operations. Here, the heat integration of the HDT process during hydrotreating of crude oil in trickle bed reactor is addressed in order to recover most of the external energy. Experimental information obtained from a pilot scale, kinetics and reactor modelling tools, and commercial process data, are employed for the heat integration process model. The optimization problem is formulated to optimize some of the design and operating parameters of integrated process, and minimizing the overall annual cost is used as an objective function. The economic analysis of the continuous whole industrial refining process that involves the developed hydrotreating (integrated hydrotreating process) unit with the other complementary units (until the units that used to produce middle distillate fractions) is also presented. In all cases considered in this study, the gPROMS (general PROcess Modelling System) package has been used for modelling, simulation and parameter estimation via optimization process. / Tikrit University, Iraq

This work suggests a new multiple ejector refrigeration cycle operated by an NGL Recovery Plant's waste heat as a replacement to the mechanical compression refrigeration cycle. This will result in significant power reduction and CO2 emission reduction. / Typical NGL plant compresses its feed to a high pressure (3040 kPa). The feed gas compressors’ discharge reaches approximately 150 OC. After that, the feed is cooled by three-stage propane vapour compression refrigeration cycle. This paper examines various options for thermal power cooling in such plants in order to eliminate part of the propane chilling system. Since most of the new plants are located in desert climates, typical designs based on absorption refrigeration are not very efficient. Design proposed in this work employs ejector refrigeration and it is based on 45 OC air as a cooling media (summer conditions in hot climates). Performance factor has been defined as the total cooling provided by the refrigeration system over the total cooling required in the 1st cooling stage of the NGL Recovery Plant. Cooling based on a single N-pentane ejector cycle with N-pentane has COP of 0.342 and performance factor (ƞ) of 0.842. Multistage ejector N-pentane refrigeration system has COP of 0.714 and performance factor (ƞ) of 1.053. For a typical 750 Million scf/d NGL plant, the new design saves $12 Millions in capital costs and $1.5 in annual electricity cost. / Thesis / Master of Applied Science (MASc)

De 20 största massabruken i Sverige släpper tillsammans ut ungefär 20 miljoner ton CO2 per år. Dessa utsläpp har biogent ursprung och anses därför vara klimatneutrala. Massa- och pappersindustrin är därmed en lämplig kandidat för implementeringen av BECCS (eng. Bioenergy with Carbon Capture and Storage) och har en betydande potential att nå de, av den svenska regeringen, uppsatta klimatmålen som säger att Sverige inte ska några nettoutsläpp av växthusgaser till atmosfären senast år 2045. I detta examensarbete simulerades kemiska absorptions- och desorptionsprocesser med MEA som lösningsmedel genom att tillämpa den hastighetsbaserade metoden i en rigorös modell i Aspen Plus. Stripper- och absorptionsmodellerna validerades innan standardprocessen modifierades till en konfiguration som möjliggör värmeintegration av koldioxidinfångningens överskottsvärme med, exempelvis, ett sulfatmassabruk. Avskiljningsgraden och laddning hos den mättade lösningen användes som prestandaindikatorer för att validera absorptionskolonnerna. Återkokarens energiåtgång och laddning hos den omättade lösningen användes somprestandaindikatorer för att validera stripperkolonnerna. Samtliga kolonner dimensionerades för att erhålla 90 vikt% avskiljningsgrad. Olika flödeshastigheter av lösningsmedlet testades för att säkerställa effektivt nyttjande av packningen i absorptions- och stripperkolonnerna. Lämpliga temperaturnivåer för värmeintegration, inom och utanför, koldioxidinfångningen erhölls genom att utvärdera olika varianter av en stripper-overhead-kompression konfiguration. Utvärderingen av den modifierade MEA processen tog hänsyn till potentialen för ångbesparing och energieffektivisering. Resultat från simuleringarna tyder på att den modifierade strippern skulle kunna ge besparingar på upp emot 11 % i ånganvändning. Energibesparingar i samma storleksordning kunde även erhållas genom värmeintegration mellan koldioxidinfångningen och en särskild process i ett referensbruk. Implementering av BECCS-konceptet på det här sättet skulle därmed kunna bli ett mer attraktivt alternativ för den svenska massa- och pappersindustrin att bekämpa klimatförändringarna. / The 20 largest pulp mills in Sweden emit around 20 million tonnes of CO2 per year. These emissions are considered carbon-neutral since they originate from biogenic sources. The pulp and paper industry is therefore a good candidate for the application of BECCS (Bioenergy with Carbon Capture and Storage) and has the potential to play a significant role for reaching the long-term mitigation target set by the Swedish government that Sweden should be climate-neutral by year 2045. In this thesis, a MEA-based chemical absorption and desorption process was rigorously modelled in Aspen Plus using the rate-based method. Validation of the absorber and stripper model was conducted before the standard process was modified to a configuration that enables heat integration of a significant amount of excess heat from the capture process in, for example, a Kraft pulp mill. CO2 removal rate and rich solvent loading were used as performance indicators to validate the absorber columns. The reboiler duty and lean solvent loading served as performance indicators in the stripper validation. The columns were dimensioned considering 90 wt% capture rate. Efficient use of the entire packing in the absorber and stripper columns was ensured by testing different solvent flow rates. Suitable temperature levels for heat integration, within and across the capture plant, were obtained through an assessment of different versions of a stripper overhead compression configuration. The evaluation of the modified MEA processes took into account the steam conservation potential and energy efficiency potential. The simulation results indicate that the modified stripper may lead to savings of up to 11% in steam consumption. Heat integration between the capture plant and a specific process in a reference Kraft pulp mill resulted in energy savings of the same order of magnitude. Thereby, making the BECCS concept a more attractive solution for the Swedish pulp and paper industry to mitigate climate change.

In this thesis, the potential to purify water utilizing waste heat from a unit which stores thermal energy and converts it to electricity is studied. The unit, called TES.POD, is developed by Azelio AB and is in this thesis used as a heat source to drive an air gap membrane distillation (AGMD) unit developed by Scarab Development AB. Heat from the TES.POD and ambient air temperature constitutes a temperature difference over a membrane used as a driving force to vaporize a part of the water that transfer through the membrane, and later condensates as clean distilled water as the contaminations stays in the hot stream of feed water. An analysis has been conducted to determine quasi-steady performance of the combined system for estimating the amount of purified water that can be supplied when the TES.POD unit is in peak electricity discharge mode. The 26 kW of waste heat accessible from the TES.POD is shown to enable two AGMD-modules producing purified water at a production of 7, 1l/h per unit having the feed water at 50°C and cooling water at 25°C. A correlation between the amount of waste heat and distilled water production is determined, as the TES.POD could be configured to produce less electricity and more waste heat at a higher temperature. The correlation showed that an 9% increase in cooling temperature, lead to an 30% increase in pure water output and a 33% decrease in electricity output. The results show that when implementing the two companies’ units together, a system that both provides electricity and distilled water is obtained. This is a system with a high demand, especially in off-grid areas with lack of both resources but with accessible renewable energy sources. Moreover, by using waste heat to purify water, it can also reduce the production cost compared to cases where conventional energy sources are used. The potential revenue of the production was estimated to 673 790 SEK/year with an implementation cost of 93 861 SEK with yearly operational expenses estimated to 14 080 SEK/year. / I detta arbete undersöks möjligheten att rena vatten med spillvärme från ett system vilket lagrar termisk energi och av den producerar elektricitet, när det behövs. Systemet är utvecklat av Azelio AB och har produktnamnet TES.POD. Vattendestillationen utförs med en så kallad air gap membrane distillation (AGMD) modul, utvecklad av Scarab Development AB. Värmen från TES.POD och omgivningstemperaturen utgör, i AGMD-modulen, en temperaturdifferens vilken i sin tur skapar en partielltryckskillnad över membranet. Denna partielltryckskillnad låter en del av det förorenade vattnet som flödar i AGMD-modulen att förångas och passera genom membranet. Föroreningarna stannar kvar i det strömmande vattnet och ångan kondenserar som renat vatten.  Arbetet visar att de 26kW som finns att tillgå i form av spillvärme är tillräckligt för att driva två AGMD-moduler att producera 7,1 l/h destillerat vatten per modul. Detta är under förutsättningar att det förorenade vattnet är 50°C och kylvattnet är 25°C. I rapporten återfinns också ett samband mellan mängden spillvärme och produktionen av destillerat vatten, eftersom TES.POD kan konfigureras till att producera spillvärme vid en högre temperatur. Sambandet visade på att 9% ökning av spillvärmens temperatur motsvarar 30% ökning i produktionen av destillerat vatten och en minskad elektricitetsproduktion på 33%.  Resultatet visar på att integrationen av dessa två produkter bildar ett system som både producerar rent vatten och elektricitet när så önskas. Detta system har till synes en stor efterfrågan, speciellt i områden utanför fast el- och vattennätverk men med goda förnyelsebara energikällor. Dessutom, eftersom vattendestillationen sker med spillvärme, kan produktionskostnaderna vara lägre än då konventionella energikällor används. Den potentiella inkomsten från produktionen estimeras till 673 790 SEK/year med en inköpskostnad om 93 861 SEK samt årliga omkostnader om 14 080 SEK/year.

See file / Se bif. fil