After the extension of the boiler 6 at Högdalenverket during 2010, there has been some problems in the form of increased carbon monoxide levels. There may be several explanations for this problem, which means that complete combustion doesent take place. There have also been problems with the ash-handling system and the sand returning systemt, this results in higher operating costs because it requires a higher consumption of inert material.The project was first divided into two phases, the first phase was to develop material and energy balances for the boiler but also introduce the parameters that we wanted to investigate further in order to possibly identify the causes of the problems that the boiler had. In the second phase experiments were going to be designed in consultation with the contact staff at Fortum to explore these parameters.During the project changes have been made in the project description, as it will require more time and more accurate planning to perform  the desired tests on the boiler. Three proposals on parameters that could be the cause of carbon monoxide problem was presented at the end of phase one and it was found that two of the proposals was not possible to carry out during the project because it would have affected economically and the availibility of the boilier.The third parameter, the bed quality effect on combustion experiment was designed in consultation with those responsible at Fortum.This experiment could also not be performed as there was some operational difficulties with the boiler during the project time. Instead, a description of the design for the experiment has been added to this project, which may at a later stage be used to investigate the bed quality impact on the carbon monoxide issues.Recent changes to the project description meant that purpose instead was to further develop the computational program created during the project's first phase and at the end of the project shall be submitted to the operators at Fortum. This calculation program takes into account the significant parameters that the boiler regulator is governed by today. The simulation program is developed using Microsoft Excel and is based on material and energy balances. This program can be used internally by Fortum to get an idea of ​​how the different mass flow rates would vary at different operating conditions and how the energy balance for the boiler would look like during the changes.When compared with materials and energy made by the boiler supplier revealed that the deviations are very small compared to what the program come up with and is caused mainly due to the assumptions made. These assumptions can be eliminated by performing experiments and collecting more data.The results gained by the calculation program has been compared with the results that was presented by the supplier during their boiler mapping, comparisons have been made regarding flue gas flows, fuel flows, combustion air flow, ash production and energy balances. It has apperad that the deviations are relatively small and the presented scheme provides a theoretical overall perspective of the boiler in line with reality.Although discussions have taken into consideration for the problem of elevated levels of carbon monoxide, and whether the measurement program can be developed further in the future. / Efter ombyggnationen av panna 6 vid Högdalenverket under år 2010, har det uppkommit en del problem i form av förhöjd kolmonoxid halt. Det kan finnas ett flertal förklaringar till problemet som innebär att fullständig förbränning inte sker. Det har även varit problem med askhanteringssystemet och sandåterföringen som inte fungerat som den ska, detta medför högre driftkostnader då det kräver en högre förbrukning av inertmaterial.   Projektet var indelat i två faser, där den första fasen var att ta fram material- och energibalanser på pannan men också presentera de parametrar som man ville undersöka vidare för att möjligen identifiera orsakerna till de problem som pannan haft.  I den andra fasen skulle experiment utformas i samråd med ansvariga från Fortum för att undersöka dessa parametrar. Under projektets gång har ändringar fått göras på projektbeskrivningen, då det krävs mer tid och noggrannare planering för att utföra test på pannan. Tre förslag på parametrar som kunde vara orsaken för CO problemen presenterades i slutet av fas ett och det konstaterades att två av förslagen inte gick att utföra under projektets gång på grund av både ekonomiska och driftrelaterade orsaker. Den tredje parametern bädd kvaliténs påverkan på förbränningen bestämdes i samråd med ansvariga i Fortum att utföras. Detta experiment kunde dock inte utföras då det uppstod vissa driftrelaterade svårigheter med pannan under projektets gång. Istället har en beskrivning av utförandet av experimentet lagts till detta projekt, som kan vid ett senare skede användas för att undersöka bädd kvaliténs påverkan på CO-halten. Nya ändringar av projektbeskrivningen innebar att syftet istället blev att vidareutveckla det beräkningsprogram som skapats under projektets första fas och som vid projektets slut ska överlämnas till de driftansvariga på Fortum. Detta beräkningsprogram tar hänsyn till de betydande parametrar som pannan regleras genom idag. Beräkningsprogrammet är framtaget med hjälp av Microsoft Excel och är grundat på material- och energibalanser. Detta program kan användas internt inom Fortum för att få en fingervisning på hur de olika massflödena skulle variera vid olika driftfall samt hur energibalansen för pannan då skulle se ut.   Vid jämförelse med material- och energibalans som gjorts av pannleverantören framgick det att avvikelserna är väldigt små jämfört med det vi framtagit, samt att det beror främst på de antaganden som gjorts. Dessa antaganden kan elimineras genom att utföra experiment och få in mer data. Resultatet som fåtts av beräkningsprogrammet har jämförts med det resultat pannleverantören fick vid sin pannkartering med hänsyn till rökgasflöde, bränsleflöden, förbränningsluft flöde, askproduktion och energibalanser. Det har framkommit att avvikelserna är relativt små och det framtagna programmet ger ett teoretiskt helhetsperspektiv av pannan som överensstämmer med verkligheten. Även diskussioner har förts till åtgärder för problemet med förhöjda halter av kolmonoxid, samt huruvida beräkningsprogrammet kan vidareutvecklas i framtiden.

Superheaters suffer large material loss during combustion of waste and biomass, causing a short life time for these expensive components. During combustion, corrosive ash particles are formed and erosion is caused by circulating bed material and sand particles, all contributing to the material loss. This study examines whether corrosion or erosion has the largest effect on this material loss by investigating two superheaters in loop seal during biomass and waste combustion of an 85 MW, Circulating Fluidized Bed (CFB) boiler in Händelö. The samples were investigated by SEM/EDX and XRD with regard to material loss and corrosion products. The superheaters have different thermal conditions since the material temperature in the first superheater that the steam passes is lower than in the one that comes after. In this report, a model to determine the tube temperature in steam boiler superheaters is also described due to the fact that the local tube temperature is of great importance of condensation of corrosive gases such as KCl and NaCl. Material loss was significantly greater on the cooler superheater compared with the warmer. The material temperatures on the outside of the tubes, were calculated to be about 574 °C for the cooler superheater and about 617°C for the warmer superheater. Overall, all analyzes showed low levels of corrosive substances, although there was a certain corrosion tendency, which indicates that material loss of the superheaters is caused by corrosion-assisted erosion. Lower material temperature of the superheater resulted in a higher degree of condensation of corrosive species such as alkali chlorides, which might have accelerated the erosion. The conclusion is that the dominant mechanism of material loss on the superheaters is erosion.

Sampling of an emplaced creosote source installed below the water table at CFB Borden was conducted over a period of ten years, with over nine thousand samples taken from approximately 250 multilevel samplers. This extensive dataset was used in several attempts to model the multi-chemical plumes emanating from this emplaced source, and to further understand the chemical and biological processes affecting these plumes and their natural attenuation. An aerobic microcosm study of naphthalene, 1-methylnaphthalene and acenaphthene was conducted in order to determine the possibility of interactions between these three chemicals. All three chemicals degraded within the eight days of the study, and the degradation of naphthalene and 1-methylnaphthalene was not affected by the presence of any of the three chemicals studied. Acenaphthene degraded more quickly when naphthalene was present in the microcosm. The programs Visual MODFLOW and RT3D were used to model the transport and degradation of naphthalene at CFB Borden. Both a first order rate reaction module and a multiple electron acceptor reaction module were used, and contaminant mass was introduced to the model through a fence of observed concentrations. Good results were found at early time with the multiple electron acceptor reaction package, however at late time the model did not match to observations. The program BIONAPL/3D was used in a similar attempt to model the transport and degradation of naphthalene. Naphthalene mass was introduced to the model through a fence of observed concentrations, and multiple electron acceptors were used to degrade this chemical. Results were good at early time, but at late time the model did not match observations. BIONAPL was then used to simulate the dissolution of the original source NAPL. Several chemicals of interest were examined: naphthalene, m-xylene, 1-methylnaphthalene and acenaphthene. Naphthalene and m-xylene dissolved from the source at rates similar to observations, however the dissolution of 1-methylnaphthalene and acenaphthene was not as well modeled. As with the Visual MODFLOW model, the BIONAPL model which best matched observations generally worked well at early times, but did not at late times. The models were not able to successfully simulate many processes that occur in the field, such as chemical and biological interactions and NAPL source dissolution. Mismatches between the models and observations are likely due to these reasons. It may be that we do not fully understand these processes, so we are unable to model them.

Sampling of an emplaced creosote source installed below the water table at CFB Borden was conducted over a period of ten years, with over nine thousand samples taken from approximately 250 multilevel samplers. This extensive dataset was used in several attempts to model the multi-chemical plumes emanating from this emplaced source, and to further understand the chemical and biological processes affecting these plumes and their natural attenuation. An aerobic microcosm study of naphthalene, 1-methylnaphthalene and acenaphthene was conducted in order to determine the possibility of interactions between these three chemicals. All three chemicals degraded within the eight days of the study, and the degradation of naphthalene and 1-methylnaphthalene was not affected by the presence of any of the three chemicals studied. Acenaphthene degraded more quickly when naphthalene was present in the microcosm. The programs Visual MODFLOW and RT3D were used to model the transport and degradation of naphthalene at CFB Borden. Both a first order rate reaction module and a multiple electron acceptor reaction module were used, and contaminant mass was introduced to the model through a fence of observed concentrations. Good results were found at early time with the multiple electron acceptor reaction package, however at late time the model did not match to observations. The program BIONAPL/3D was used in a similar attempt to model the transport and degradation of naphthalene. Naphthalene mass was introduced to the model through a fence of observed concentrations, and multiple electron acceptors were used to degrade this chemical. Results were good at early time, but at late time the model did not match observations. BIONAPL was then used to simulate the dissolution of the original source NAPL. Several chemicals of interest were examined: naphthalene, m-xylene, 1-methylnaphthalene and acenaphthene. Naphthalene and m-xylene dissolved from the source at rates similar to observations, however the dissolution of 1-methylnaphthalene and acenaphthene was not as well modeled. As with the Visual MODFLOW model, the BIONAPL model which best matched observations generally worked well at early times, but did not at late times. The models were not able to successfully simulate many processes that occur in the field, such as chemical and biological interactions and NAPL source dissolution. Mismatches between the models and observations are likely due to these reasons. It may be that we do not fully understand these processes, so we are unable to model them.

Purpose of this study was to investigate the possibilities of using Near-infrared (NIR) spectroscopy to detect glass in refuse derived fuel (RDF) as well as what on-line data of glass content could be used for in terms of boiler operation and performance determination. Sample configurations were done with dried RDF (to prevent mass loss due to moisture and spectroscopic disturbance) and increasing concentrations of colored soda-lime glass, total of 100 samples. Glass was randomly scattered among the RDF by shaking the added glass and RDF in a bucket to generate representative samples of real life conditions. NIR-spectra acquisition was done between 12000 and 4000 cm-1, at 8 cm-1 resolution and average of 32 scans. The determination of boiler performance was done in accordance to Swedish standards for acceptance testing and heat loss due to glass was treated as slag. Resulting performance calculations showed boiler efficiency via indirect method matching efficiency calculated via direct method (deviating at maximum 2 %) which validates the summarized losses (including due to glass). The heat loss due to glass was calculated to 0,068 MW/%glass, which equated to average of 0,16 MW for 2,37 % glass. Total heat loss was amounted to an average of 11,53 MW. The developed models were not satisfactory in their quality of regression prediction. Although some had, through pre-processing, good development of explained variance at increasing factors, but still had a “Not Applicable” coefficient of determination by regression prediction. The poor quality of models can be explained by poor glass detection (poor representation) of the spectroscopic instrument due to a combination of glass being randomly scattered in the background material and sometimes covered by RDF as well as that the NIR-spectroscopy light beam only hits a small area. By increasing the number of samples upwards 300 -500, the effect of random scatter of glass can be mitigated and acceptable models could be acquired. / FUDIPO

A methodology for the thermodynamic-kinetic evaluation of circulating systems as TSA carbon capture processes is developed and used in the assessment of a novel CFB configuration against a benchmark (co-current riser). The novel CFB features a counter-current adsorber, a counter-current regenerator and a riser, the latter element playing a double role of solids conveyer and co-current adsorber. The advantages sought by using a counter-current adsorber are not only the more efficient gas-solid contact mode with respect co-current, but also a low pressure drop derived from operation at lower gas velocities and hydrostatic head partially supported on the contactor internals. Knowledge of the adsorption equilibrium alone is sufficient to realise the much higher sorbent circulation rates required by co-current configurations –compared to counter-current– to meet the stringent carbon capture specifications of 90% recovery and 95% purity. Higher solids circulation rates imply higher energy requirements for regeneration, and therefore research and development of co-current gas-solid contactors cannot be justified in terms of searching for energy-efficient post-combustion carbon capture processes. Parallel experimental investigation in the operation and fluid dynamics of cold model CFB rigs is carried out with the purposes of: 1) providing information that may impact the process performance and can be fed into the mathematical model used in the theoretical assessment for more realistic evaluation, and 2) determine gas and solids residence time distributions (RTDs), which are used for the estimation of axial dispersion and comparison with published results in similar systems. Gas RTD data is generated using a tracer pulse injection-detection technique, whereas RTD for the solid phase is studied using positron emission particle tracking (PEPT). The PEPT technique proved to be adequate for the identification of flow regimes in the novel design of the counter-current adsorber, featuring inclined orifice trays. At low gas velocities the particles flow straight down through the tray holes, whereas at higher velocities the particles flow down in zig-zag, increasing the residence time of the particles and reducing the particle axial dispersion, both beneficial in terms of separation efficiency.

Many particulate processes are preferably implemented in circulating fluidized beds (CFB) over traditional low-velocity fluidization to take advantage of the many benefits of circulating systems. Fluid catalytic cracking (FCC) is one of the most successfully applied processes in CFB technology, with more than 350 FCC units in operation worldwide. Despite its extensive use, an understanding of the complex behaviour of these units is incomplete.<p> A theoretical and experimental evaluation of the fluidization behaviour was conducted in the CFB riser, standpipe, and stripper. Initially, an extension of the existing CFB in the Fluidization Laboratory of Saskatchewan was designed. The experimental program conducted in this study included an examination of the solids flow behaviour in the riser, interstitial gas velocity in the downcomer, and stripping efficiency measurements. The hydrodynamic behaviour of the stripper was modeled using Multiphase Flow with Interphase eXchanges (MFIX) CFD code.<p> The solids flow behaviour in the bottom zone of a high-density riser was investigated by measuring the local upwards and downwards solids flux. Solids circulation rates between 125 and 243 kg/(m2⋅s) were evaluated at a constant riser superficial gas velocity of 5.3 m/s. The effect of the riser superficial gas velocity of the local upflow at the riser centerline was also conducted at a solids circulation rate of 187 kg/(m2⋅s). The results show that there is little variation in the local net solids flux at radial locations between 0.00 ¡Ü r/R ¡Ü 0.87. The results indicate that a sharp regime change from a typical parabolic solids flux profile to this more radially uniform solids flux profile occurs at a gas velocity between 4.8 and 4.9 m/s.<p> To quantify stripping efficiency, the underflow of an injected tracer into the standpipe must be known. Quantification of the underflow into the standpipe requires knowledge of two main variables: the interstitial gas velocity and the tracer gas concentration profiles in the standpipe. Stripping efficiency was determined for stripper solids circulation rates of 44, 60, and 74 kg/(m2⋅s) and gas velocities of 0.1, 0.2, and 0.3 m/s. For most conditions studied, the interstitial gas velocity profile was found to be flat for both fluidized and packed bed flow. The stripping efficiency was found to be sensitive to the operating conditions. The highest efficiency is attained at low solids circulation rates and high stripping gas velocities.<p> In the numeric study, stripper hydrodynamics were examined for similar operating conditions as those used in the experimental program. Due to an improved radial distribution of gas and decreasing bubble rise velocity, mass transfer is deemed most intense as bubbles crest above the baffles into the interspace between disc and donut baffles. Stripping efficiency is thought to improve with increasing gas velocity due to an increased bubbling frequency. Stripping efficiency is thought to decrease with increasing solids circulation rates due to a lower emulsion-cloud gas interchange coefficient and a decreased residence time of the emulsion in the stripper.

Many particulate processes are preferably implemented in circulating fluidized beds (CFB) over traditional low-velocity fluidization to take advantage of the many benefits of circulating systems. Fluid catalytic cracking (FCC) is one of the most successfully applied processes in CFB technology, with more than 350 FCC units in operation worldwide. Despite its extensive use, an understanding of the complex behaviour of these units is incomplete.<p> A theoretical and experimental evaluation of the fluidization behaviour was conducted in the CFB riser, standpipe, and stripper. Initially, an extension of the existing CFB in the Fluidization Laboratory of Saskatchewan was designed. The experimental program conducted in this study included an examination of the solids flow behaviour in the riser, interstitial gas velocity in the downcomer, and stripping efficiency measurements. The hydrodynamic behaviour of the stripper was modeled using Multiphase Flow with Interphase eXchanges (MFIX) CFD code.<p> The solids flow behaviour in the bottom zone of a high-density riser was investigated by measuring the local upwards and downwards solids flux. Solids circulation rates between 125 and 243 kg/(m2⋅s) were evaluated at a constant riser superficial gas velocity of 5.3 m/s. The effect of the riser superficial gas velocity of the local upflow at the riser centerline was also conducted at a solids circulation rate of 187 kg/(m2⋅s). The results show that there is little variation in the local net solids flux at radial locations between 0.00 ¡Ü r/R ¡Ü 0.87. The results indicate that a sharp regime change from a typical parabolic solids flux profile to this more radially uniform solids flux profile occurs at a gas velocity between 4.8 and 4.9 m/s.<p> To quantify stripping efficiency, the underflow of an injected tracer into the standpipe must be known. Quantification of the underflow into the standpipe requires knowledge of two main variables: the interstitial gas velocity and the tracer gas concentration profiles in the standpipe. Stripping efficiency was determined for stripper solids circulation rates of 44, 60, and 74 kg/(m2⋅s) and gas velocities of 0.1, 0.2, and 0.3 m/s. For most conditions studied, the interstitial gas velocity profile was found to be flat for both fluidized and packed bed flow. The stripping efficiency was found to be sensitive to the operating conditions. The highest efficiency is attained at low solids circulation rates and high stripping gas velocities.<p> In the numeric study, stripper hydrodynamics were examined for similar operating conditions as those used in the experimental program. Due to an improved radial distribution of gas and decreasing bubble rise velocity, mass transfer is deemed most intense as bubbles crest above the baffles into the interspace between disc and donut baffles. Stripping efficiency is thought to improve with increasing gas velocity due to an increased bubbling frequency. Stripping efficiency is thought to decrease with increasing solids circulation rates due to a lower emulsion-cloud gas interchange coefficient and a decreased residence time of the emulsion in the stripper.

Karlstads Energi AB är ett medborgarägt företag som levererar värme och el till Karlstad med omnejd. Sedan uppförandet av det nya kraftvärmeverket Heden 3 har kraftvärmeverket Heden 2 fått förändrade driftförhållanden och körs numera ofta på låga laster under pannans drifttid vilket har resulterat i ökade NOx-utsläpp. Som energiproducent omfattas Karlstads Energi av kväveoxidavgiften och det finns en önskan om att öka marginalen för att nå miljökraven. Då NOx-utsläppen främst beror på för stort O2-överskott i pannan finns det möjlighet att ersätta en del av förbränningsluften med recirkulerade rökgaser för att minska tillgänglig O2. För att fortsätta vara relevanta på energimarknaden har Karlstads Energi ett behov av att utveckla nya tjänster och produkter. Samproduktion av syntesgas kan vara aktuellt som värdeskapande process när samhället rör sig mot en bioekonomi och det finns anledning att utvärdera hur det skulle komma att påverka förbränningsprocessen. Förbränningsprocessen inklusive rådande NOx-reducerande åtgärder i Heden 2 har modellerats i CHEMCAD. Baserat på modellen har rökgasrecirkulation samt effekterna av att samproducera syntesgas implementerats. I fallet med syntesgas ersätts en del av bränslet med förgasningskoks och värme tas ut från den externa bäddcirkulationen för att driva syntesgasreaktorn. Modellen inkluderar reaktionskinetik för NOx-bildning och -reduktion samt intern och extern bäddcirkulation. Rökgasrecirkulation fungerar som NOx-reducerande åtgärd vid drift med låg last. Beroende på bränslesammansättning kan NO-bildning minska med upp till 10% och NO-utsläpp med upp till 67%. Optimal andel recirkulerade rökgaser är 20% när flis förbränns respektive 15% vid samförbränning av förgasningskoks. Temperaturen i pannan sjunker något med ökande flöde av recirkulerade rökgaser och överstiger aldrig 800°C vilket riskerar att skapa en ineffektiv NOx-reduktion med selektiv ickekatalytisk reduktion (SNCR). Samförbränning av förgasningskoks ökar den totala effektutvecklingen med ca 1,5 MW jämfört med då endast flis förbränns och värmeuttaget från cyklonen som driver den nya syntesgasreaktorn har försumbar inverkan på bäddmaterialets temperatur. Slutsatser som dras är att rökgasrecirkulation fungerar som NOx-reducerande åtgärd vid låg last. Samproduktion av syntesgas har en NOx-hämmande effekt och kan ge ett minskat bränslebehov för att möta energibehovet.

Vätgasbildning vid behandling av flygaska är ett problem många förbränningsanläggningar hanterar. På E.ON i Norrköping har vätgasbildning lett till kraftig explosion i bergrum där flygaska deponeras, men även för askmottagare innebär vätgasbildningen risker då incidenter med självantändande askhögar inträffat. Detta examensarbete har därför fokus på att minimera dessa vätgasrelaterade risker genom att undersöka vad som påverkar vätgasbildningen i flygaskan och reaktiviteten, främst med avseende på metalliskt aluminium, i CFB-pannorna P14 och P15 på Händelöverket. Med hjälp av kvantifiering av gasbildning har maximal vätgasbildning, vätgasbildningshastigheten, pH samt vikt-% metalliskt aluminium dokumenterats. De resultat som sammanställts inkluderar olika driftstörningar och förhållanden i pannorna som påträffats under projektets tidsperiod, därav skillnad mellan pannorna, kiselsand eller ilmenit som bäddmaterial, ammoniakdosering, del-last samt avstängd NID-reaktor. Utöver detta erhölls även totalhaltanalys utfört via ICP-SFMS analys där askans sammansättning presenteras. Resultaten påvisade skillnader i vätgasbildning för flera av de olika driftstörningarna och förutsättningarna mellan pannorna men även inom en och samma panna. Aska från P15 har högre reaktivitet, det påvisades även mindre vätgasbildning vid ilmenit som bäddmaterial samt vid avstängd NID-reaktor och vid del-last. Trots dessa skillnader i vätgasutveckling drogs slutsatsen att flygaska från avfallseldande CFB-pannor inte går att påverka till den grad att det avsevärt minskar mängden metalliskt aluminium och därmed vätgasbildningen utan att separera aluminiumet innan det genomgår förbränning. / Minimering av vätgasrelaterade risker från Avfallseldande CFB-pannor