Methodology of Typical Accessory Pathway Catheter Ablation

Available online at www.sciencedirect.com ScienceDirect Energy Procedia 61 (2014) 643 – 647 The 6th International Conference on Applied Energy – ICAE2014 The experimental study of full-scale biomass-fired bubbling fluidized bed boiler Jan Skvarila,b,*, Anders Avelina, Jan Sandberga, Erik Dahlquista a b School of Bussiness Society and Engineering, Mälardalen University, Box 883, Högskoleplan 1, 721 23 Västerås, Sweden Energy Institute, Faculty of Mechanical Engineering, Brno University of Technology, Technická 2, 616 69 Brno, Czech Republic Abstract This paper presents experimental data concerning combustion characteristics of full-scale biomass-fired bubbling fluidized bed (BFB) steam boiler with a thermal output of 31 MW. The purpose of the experimental measurements is to show how the values of selected combustion parameters vary in reality depending on measurement position. Experimentation involves specifically a determination of combustion gas temperature and concentration of gas species i.e. O2, CO2, CO and NOX at different positions in the furnace and the flue gas trains. Character of results from the furnace indicates the intermediate stage of thermochemical reactions. Increased levels of CO close to the wall have been found, this may be indicating reducing atmosphere and thereby increased corrosion risk. Results from flue gas trains demonstrate that behavior there is related to the fluid dynamics and heat transfer, the temperature is too low for further combustion reactions. Results show great variations among measured values of all measurands depending on a distance along the line from the wall to the center of the boiler. The measurements from permanently installed fixed sensors are not giving value representing average conditions, but overall profiles can be correlated to online measurements from fixed sensors. © 2014 Published by Elsevier Ltd. This © 2014The TheAuthors. Authors. Published by Elsevier Ltd.is an open access article under the CC BY-NC-ND license (http://creativecommons.org/licenses/by-nc-nd/3.0/). Selection and/or peer-review under responsibility of ICAE Peer-review under responsibility of the Organizing Committee of ICAE2014 Keywords: Biomass combustion; steam boiler; fluidized bed; temperature measurements; flue gas concentration measurements. 1. Introduction Fluidized bed combustion is considered as one of the most promising techniques because of its flexibility, high combustion efficiency and low environmental impact [1]. It has been developed and tested over many decades as presented by Koornneef et al. [2]. Nevertheless there are still some issues to be studied in relation to the combustion of biomass as it is a fuel with certain specific properties that affect * Jan Skvaril. Tel.: +46-21-151738; fax: +46-21-101480. E-mail address: [email protected]. 1876-6102 © 2014 The Authors. Published by Elsevier Ltd. This is an open access article under the CC BY-NC-ND license (http://creativecommons.org/licenses/by-nc-nd/3.0/). Peer-review under responsibility of the Organizing Committee of ICAE2014 doi:10.1016/j.egypro.2014.11.1188 644 Jan Skvaril et al. / Energy Procedia 61 (2014) 643 – 647 combustion process and equipment. The combustion diagnostics in industrial applications is uncertain since the fixed sensors permanently installed in the boiler are placed in very few positions (Fig. 1.). Therefore, it is necessary to carry out an experimental work in order to get more detailed insight of the combustion process. Examination of the literature shows remarkable studies concerning full-scale steam boilers (e.g. [3-5]), however the availability of the data from biomass fired boilers is very scarce. In relation to the limited access to the data the research project was designed at Malardalen University in order to obtain comprehensive experimental diagnostic data from different full-scale biomass-fired steam boilers. The study presented here is a facet of comprehensive research project and the aim is to provide data from bubbling fluidized bed (BFB) steam boiler with a thermal output of 31 MW. Experimentation involves specifically a determination of combustion flue gas temperature and concentration of gas species i.e. O2, CO2, CO, NOX at different positions in the furnace and flue gas trains. This data will be further used for formation, development and verification of analytical and numerical mathematical models and for controlling and optimization purposes. 2. Material and methods 2.1. Experimentation The measurement procedure was designed so that the flue gases are extracted from the different points lying on the line at certain positions in the furnace (Fig. 1. Ports SHE1, SHE2), and flue gas trains (Fig 1. Ports SHE3, SHE4, SHE5). The distribution of individual measurement points on the line was proposed in accordance with the assumption that there would be steeper gradients in positions near the wall. Flue gases are drawn through the water-cooled suction pyrometer where the temperature is measured by precalibrated type K thermocouple. After passing suction pyrometer, the flue gases are further dried and purified and then pumped to the calibrated gas analyzers where the gas concentration is measured. Analyzers used are Fuji Electric ZRJ Infrared GA for O2, CO2 and CO concentration analysis and Eco Physics CLD 700 EL ht for NOx concentration analysis (both on dry gas stream). The signal from the measuring instruments is processed in the PC logger and a recorded by PC at 10 second intervals. There are approx. 90 values read for each measurand at each point. Nominal operating parameters: Thermal capacity (without FGC) Electrical output Flue gas condenser (FGC) output Nominal steam parameters: Flow rate of main steam Temperature of main steam Pressure of main steam 30.8 MWt 10 MWe 7–8 MWt 11.9 kg·s-1 480 °C 80 bar Operating parameters during experimentation: Total thermal output 25.8 MWt (± 5%) Electrical output 7.7 MWe (± 5%) FGC output 0 MWt Flow rate of main steam 10.1 kg∙s-1 (± 5%) Fuel properties during experimentation: Net calorific value 8400 kJ∙kg-1 Moisture content (as received) 54 wt% Ash content (dry matter) 1.4 wt% Composition: Forest residue chips (73 wt%), Stem wood chips (12 wt%), Sawdust (15 wt%) Fig. 1. Bubbling fluidized bed boiler 30.8 MW Jan Skvaril et al. / Energy Procedia 61 (2014) 643 – 647 2.2. Boiler design and operating parameters The BFB boiler (Fig. 1.) is used for combined heat and power production and it was constructed by Foster Wheeler AG. The furnace has evaporator membrane water walls on all four sides. The bottom membrane panel and is covered with protective refractory lining, so that bubble caps protrude and lining exceeds and covers membrane walls to a height of approx. 2.5 m from the furnace bottom. Primary air is brought to the furnace through the bottom bubble caps. Secondary air is staged and brought in at several levels along the furnace freeboard. The boiler consist of convective vertical pendant superheaters (SH I., SH II. and SH III.), economizer (ECO) and air preheaters (AP). The boiler is equipped with flue gas recirculation and a flue gas condenser (FGC). Furthermore, there are sensors permanently installed for temperature measurements (Fig. 1. T1 and T2) and O2 concentration measurements (Fig. 1. O2 1 and O2 2). These sensors are placed approx. 0.3 m from the boiler wall and are used for online process monitoring. During experiments, the boiler was operated with an emphasis on steady operating conditions. However some fluctuations were observed due to operational constrains such as variable fuel properties and fluctuating demand in district heating (for details see, Fig. 1.) Fuel fired during experiments was a mixture of solid biomass-based materials from broadleaves, conifers and shrubs (for details, see Fig. 1.). 3. Results and discussion Note that average values are used when discussing results and the positive and negative error bars in graphs represent the sample standard deviation both calculated from repeated measurements (approx. 90 values). Character of the results from the points in the furnace (Ports SHE1, SHE2) indicates the intermediate stage of thermochemical reactions. Results shows that temperature near port SHE1 increases uniformly along the line (Fig. 2.). Temperature profile is correlates negatively with O2 concentration (Fig. 3.). Whilst CO concentration is low near the wall and then abruptly rises and reaches the limit of the instrument at the distance of 2.0 m (Fig. 4.). Moreover, CO concentration is characterized by a high variation between the repetitions. NOX concentration rises evenly from point at 0.1 m to 2.0 m, and then slightly decreases at 3.0 m from the wall (Fig. 5.). Thermochemical reactions near SHE1 take place most intensively in the middle of the furnace, where the highest temperature occurs with relatively low level of excess air. Combustion intensity decreases towards the wall. Abrupt change of CO concentration at 1.0 m from the wall (Fig. 4.) suggests that secondary air flows along the boiler wall and does not fully participate on combustion in the center of the furnace and thus creates the oxidizing atmosphere near the wall. Temperature in the vicinity of port SHE2 is lower than that near SHE1; it rapidly increases from 0.1 m to 0.3 m and then rises moderately (Fig. 2.). O2 concentration is relatively high at 0.1 m then drops at 0.3 m, considerable peak is noticeable at 2.0 m from the boiler wall; at 3.0 m O2 concentration decreases (Fig. 3.). Unlike the measurements near SHE1, no significant correlation with temperature is observed. CO concentration reaches higher values at the positions of 0.1 m and 0.3 m with a subsequent decline at 1.0 m and at 2.0 m followed by an increase at 3.0 m from the boiler wall (Fig. 4.). High concentration of CO close to the wall result in increased risk of corrosion and material deterioration of boiler walls, this may reduce lifetime of equipment significantly [1]. Concentration of NOX follows “a parabolic profile” and reaches the maximum at 3.0 m from the boiler wall (Fig. 5.). As near port SHE1, the most thermochemical reactions take place in the center of the furnace and combustion intensity decrease towards the wall. It is evident that a significant reduction in temperature at 0.1 m is accompanied by a high concentration of O2 and CO. This indicates poor combustion efficiency, where the O2 is not fully utilized and the carbon from the fuel is not completely converted into CO 2. With increased CO we can 645 646 Jan Skvaril et al. / Energy Procedia 61 (2014) 643 – 647 also expect a higher content of pyrolysis products especially on particle surfaces. 1000 900 SHE1 partial load SHE2 partial load Centerline 800 700 0 1000 2000 3000 Distance from the wall (mm) 4000 Fig. 2. Temperature profile – side walls of the furnace CO concentration (ppm) 2000 SHE1 partial load SHE2 partial load Centerline 1500 10 9 8 7 6 5 4 3 2 O2 concentration (vol%) 1100 1000 500 SHE1 partial load SHE2 partial load Centerline 0 90 70 SHE1 partial load SHE2 partial load Centerline 50 30 1000 2000 3000 Distance from the wall (mm) 0 4000 Fig. 4. CO concentration profile – side walls of the furnace 2000 3000 4000 Distance from the wall (mm) 110 0 0 1000 Fig. 3. O2 concentration profile – side walls of the furnace NOX concentration (ppm) Temperature (°C) 1200 1000 2000 3000 Distance from the wall (mm) 4000 Fig. 5. NOX concentration profile – side walls of the furnace Results show that behavior in flue gas trains is related to the fluid dynamics and heat transfer, the temperature is too low for further combustion reactions [6]. The results of measurements in ports SHE3, SHE4 and SHE5 show that the flue gas temperature is distributed unevenly over the line (Fig. 6.). The highest temperature is reached at the distance of 0.1 m (SHE3, SHE4) and 0.35 m (SHE5). The cause of uneven temperature distribution over the line (approximately 50 °C along the line) is asymmetrical air supply due to the AP design. Profile measured next to the port SHE3 shows an abrupt increase of the concentration of O2 at the distance of 0.35 m from the wall (Fig. 7.). It can be largely explained by the leakage in the air preheater 3 for primary air. This hypothesis is also supported by diluted concentration of CO and NOX in comparison with concentrations near SHE4 and SHE5. Great variations of presented values near the port SHE3 are caused by changes in operating conditions in relation to the shutdown of the turbine. SHE3 partial load SHE4 partial load SHE5 partial load Centerline 250 225 200 175 6 O2 concentration (vol%) Temperature (°C) 275 5 SHE3 partial load SHE4 partial load SHE5 partial load Centerline 4,5 4 3,5 150 Fig. 6. Temperature profile – air preheaters 1000 600 500 1000 1500 2000 Distance from the wall (mm) Fig. 7. O2 concentration profile – air preheaters SHE3 partial load SHE4 partial load SHE5 partial load Centerline 800 0 500 1000 1500 2000 Distance from the wall (mm) 400 200 0 NOX concentration (ppm) 0 CO concentration (ppm) 5,5 75 55 SHE3 partial load SHE4 partial load SHE5 partial load Centerline 35 15 0 500 1000 1500 Distance from the wall (mm) 2000 Fig. 8. CO concentration profile – air preheaters 0 500 1000 1500 2000 Distance from the wall (mm) Fig. 9. NOX concentration profile – air preheaters Jan Skvaril et al. / Energy Procedia 61 (2014) 643 – 647 In summary, results from the performed experimental measurements vary greatly along the line from the wall to the center, therefore the results from fixed sensors permanently installed can’t be considered as entirely representative (e.g. temperature at SHE1 is significantly higher at 3.0 m compare to the values at 0.3 m from the wall). If we assume that our experimental results show correct absolute values, profiles such as these can be correlated with measurements from fixed sensors permanently installed in the boiler to improve control in comparison to only using the data from fixed sensors. 4. Conclusions Experimental measurements (i.e. combustion flue gas temperature and concentration of O 2, CO2, CO, and NOX) were carried out at different points in the full-scale biomass-fired bubbling fluidized bed boiler. Results of the constructed profiles from the furnace indicates the intermediate stage of thermochemical reactions and show that the thermochemical reactions peak at the center of the furnace and combustion intensity decrease towards the wall. Furthermore, increased levels of CO concentration close to the wall has been found in the vicinity of port SHE2. This maybe indicating reducing atmosphere and thereby increased corrosion risk. Results of the constructed profiles from flue gas trains shows that behavior there relates mainly to fluid dynamics and heat transfer. The temperature is too low for further combustion reactions. Asymmetrical cooling of flue gases in flue gas duct was found and a leakage has been identified in the air preheater 3. Moreover, it is evident that there are great variations among measured values of all measurands depending on a distance along the line from the wall to the center of the boiler. This indicates that the measurements from fixed sensors are not giving value representing the average conditions, however overall profiles can be correlated to online measurements from fixed sensors. References [1] Khan AA, de Jong W, Jansen PJ, Spliethoff H. Biomass combustion in fluidized bed boilers: Potential and Remedies. Fuel Processing Technology 2009;90(1): 21-50. [2] Koornneef J, Junginger M, Faaij A. Development of fluidized bed combustion – An overview of trends, performance and cost. Science PiEaC 2007; 19-55. [3] Costa M, Azevedo JLT. Experimental Characterization of an Industrial Pulverized Coal-Fired Furnace Under Deep Staging Conditions. Comb Sci. and Tech 2007;179(9):1923-35. [4] Kuang M, Li Z, Zhang Y, Chen X, Jia J, Zhu Q. Asymmetric combustion characteristics and NOx emissions of a down-fired 300 MWe utility boiler at different boiler loads. Energy 2012;37(1):580-90. [5] Li Z, Liu G, Zhu Q, Chen Z, Ren F. Combustion and NOx emission characteristics of a retrofitted down-fired 660 MWe utility boiler at different loads. Applied Energy 2011;88(7):2400-6. [6] Baukal CE. Industrial combustion testing. Taylor & Francis; 2011. Biography Jan Skvaril is a PhD student at Mälardalen University, Sweden. He holds a master’s degree in Mechanical Engineering and master’s degree in Economics and Management, both from Brno University of Technology. Currently he is studying fluid dynamics with emphasis on how temperatures are distributed in different types of furnaces. 647