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Academic literature on the topic 'Fluidized Catalytic Cracker Units'

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Published: 4 June 2021
Last updated: 19 February 2023

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Journal articles on the topic "Fluidized Catalytic Cracker Units"

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WHITCOMBE, J. M., I. E. AGRANOVSKI, R. D. BRADDOCK, F. GANDOLA, and A. P. HAMMOND. "CATALYST FRACTURE DUE TO THERMAL SHOCK IN FLUIDIZED CATALYTIC CRACKER UNITS." Chemical Engineering Communications 191, no. 11 (November 2004): 1401–16. http://dx.doi.org/10.1080/00986440490464165.

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Agranovski, I. E., J. M. Whitcombe, and M. Swiericzuk. "STUDY OF EMISSION RATE FROM FLUIDIZED CATALYTIC CRACKER UNITS DURING START UP SITUATIONS." Journal of Aerosol Science 32 (September 2001): 625–26. http://dx.doi.org/10.1016/s0021-8502(21)00285-8.

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Souza, J. A., J. V. C. Vargas, O. F. Von Meien, and W. P. Martignoni. "MODELING AND SIMULATION OF INDUSTRIAL FCC RISERS." Revista de Engenharia Térmica 6, no. 1 (June 30, 2007): 19. http://dx.doi.org/10.5380/reterm.v6i1.61812.

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Risers are considered vital parts in Fluidized Catalytic Cracking (FCC) conversion units. It is inside the riser reactor that the heavy hydrocarbon molecules are cracked into lighter petroleum fractions such as liquified Petroleum gas (LPG) and gasoline. The FCC process is considered a key process in the world petroleum industry, since it is the main responsible for the profitable conversion of heavy gasoil into commercial valuable products. This work presents a simplified transient model to predict the response of a FCC riser reactor, i.e., the fluid flow, temperature and concentrations of the mixture components throughout the riser and at the exit. A bi-dimensional fluid flow field combined with a 6 lumps kinetic model and two energy equations are used to model the gasoil mixture flow and the cracking process inside the riser reactor. The numerical results are in good agreement with experimental data, as a result, the model can be utilized for design, and optimization of FCC units. The simulation herein presented shows the applicability of the proposed method for the numerical simulation and control of industrial riser’s units.
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Pereira, A. H. A., D. Y. Miyaji, M. D. Cabrelon, J. Medeiros, and J. A. Rodrigues. "A study about the contribution of the α-β phase transition of quartz to thermal cycle damage of a refractory used in fluidized catalytic cracking units." Cerâmica 60, no. 355 (September 2014): 449–56. http://dx.doi.org/10.1590/s0366-69132014000300019.

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The deterioration of refractories used in fluidized catalytic cracking units (FCC-units) is responsible for high costs of maintenance for the petrochemical industry. This is commonly associated with coke deposition during the production of light hydrocarbons. However, other mechanisms responsible for causing damage may also occur, such as the generation of cracks by expansive phase transition. The aim of the work herein was to study the contribution of the a-b phase transition of quartz particles to the deterioration of a commercial aluminosilicate refractory used in a riser by the means of slow thermal cycles. Such damage may occur if the working temperature of the equipment fluctuates around the a-b transition temperature (573 °C). The current study considered the material with and without coke impregnation to evaluate the combined effect of coke presence and phase transition. To evaluate the damage, it was used the Young's modulus as a function of temperature by applying the Impulse Excitation Technique under controlled atmosphere. An equipment recently developed by the authors research group was applied. Specimens were prepared and submitted to slow thermal cycles of temperatures up to 500 °C and up to 700 °C, with a heating rate of 2 °C/min. Part of the specimens was previously impregnated with coke by a reactor using propen. To complete the evaluation, characterization by X-ray diffraction, as well as by dilatometry and scanning electron microscopy were performed. The findings of this study showed that the presence of quartz particles determine the thermo-mechanical behaviour of the material, as well as the thermocycling damage resistance. In spite of the fact that the a-b phase transition stiffens the material during the heating stage, it increases the damage by slow thermal cycling. The coke impregnation increases the resistance to slow thermal cycles, however it decreases the resistance to the damage evolution.
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Palazoglu, Ahmet, and Tanes Khambanonda. "Dynamic operability analysis of a fluidized catalytic cracker." AIChE Journal 33, no. 6 (June 1987): 1037–40. http://dx.doi.org/10.1002/aic.690330618.

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Cooper, D. A., and A. Emanuelsson. "Nitrogen oxide (N2O) emissions from a fluidized-bed catalytic cracker." Energy & Fuels 6, no. 2 (March 1992): 172–75. http://dx.doi.org/10.1021/ef00032a009.

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Boum, Alexandre, Jean Pierre Corriou, and Abderrazak Latifi. "Comparison of model predictive control strategies for a fluidized catalytic cracker." International Journal of Engineering & Technology 6, no. 4 (November 28, 2017): 181. http://dx.doi.org/10.14419/ijet.v6i4.7641.

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A FCC model is used to compare five different Model Predictive Control (MPC) strategies. The FCC process is a complex petrochemical unit with catalyst recycling that makes its behaviour highly nonlinear. The FCC comprises a riser, a separator and a regenerator with important heat coupling due to the endothermic cracking reactions of gas oil in the riser and the exothermic combustion reactions in the regenerator. The riser and the regenerator exhibit fast and slow dynamics respectively. The temperatures at riser top and in the regenerator should be controlled by manipulation of catalyst and air flow rates. All these nonlinear and coupled characteristics render the multivariable control problem difficult and thus the FCC process constitutes a valuable benchmark for comparing control strategies. Here, the performances of Dynamic Matrix Control, Quadratic Dynamic Matrix Control, MPC control with penalty on the outputs, NonLinear MPC control, Observer Based MPC control are compared.
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Sarma, Pramit, and Raghunathan Rengaswamy. "Multivariable gain-scheduled fuzzy logic control of a fluidized catalytic cracker unit." Computers & Chemical Engineering 24, no. 2-7 (July 2000): 1083–89. http://dx.doi.org/10.1016/s0098-1354(00)00487-7.

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Rajeev, N., R. Krishna Prasad, and U. B. Reddy Ragula. "Process Simulation and Modeling of Fluidized Catalytic Cracker Performance in Crude Refinery." Petroleum Science and Technology 33, no. 1 (December 8, 2014): 110–17. http://dx.doi.org/10.1080/10916466.2014.953684.

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Souza, J. A., J. V. C. Vargas, J. C. Ordonez, W. P. Martignoni, and O. F. von Meien. "Thermodynamic optimization of fluidized catalytic cracking (FCC) units." International Journal of Heat and Mass Transfer 54, no. 5-6 (February 2011): 1187–97. http://dx.doi.org/10.1016/j.ijheatmasstransfer.2010.10.034.

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Dissertations / Theses on the topic "Fluidized Catalytic Cracker Units"

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Whitcombe, Joshua Matthew, and n/a. "Study of Catalyst Particle Emissions From a Fluidized Catalytic Cracker Unit." Griffith University. School of Environmental Engineering, 2003. http://www4.gu.edu.au:8080/adt-root/public/adt-QGU20031003.152200.

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The control of particle emissions from an oil refinery is often difficult, due to changing operational conditions and the limited range of available treatment options. Excessive particle emissions have often been attributed start up problems with Fluidized Catalytic Cracker Units (FCCU) and little information is available regarding the exact composition and nature of these excessive emissions. Due to the complex nature of a FCCU, it has in the past been difficult to identify and control emissions, without the use of expensive end of pipe technologies. An Australian Oil Refinery, concerned with their catalyst emissions, sponsored this study of FCCU particle emissions. Due to the industrial nature of the project, a holistic approach to the management of emissions was taken, instead of a detailed investigation of a single issue. By looking at the broader range of issues, practical and useful outcomes can be achieved for the refinery. Initially, detailed emissions samplings were conducted to investigate the degree of particle emissions under start up conditions. Stack emissions were collected during a standard start up, and analysed to determine the particle size distribution and metal concentration of the emitted material. Three distinct stages of emissions were discovered, initially a high concentration of larger particles, followed by a peak in the very fine particles and finally a reduction of particle emissions to a more steady or normal operational state. The variation in particle emissions was caused by operational conditions, hardware design and catalyst characteristics. Fluctuations in the gas velocity through the system altered the ability of the cyclones to collect catalyst material. Also, the low bed level allowed air bypass to occur more readily, contributing to the increased emissions levels seen during the initial stage of the start up. Reduced fluidity characteristics of the circulating catalyst also affected the diplegs operations, altering the collection efficiency of the cyclone. During the loading of catalyst into the system, abraded material was quickly lost due to its particle size, contributing to fine particle emissions levels. More importantly, thermal fracturing of catalyst particles occurred when the cold catalyst was fed into the hot regenerator. Catalyst particles split causing the generation of large amounts of fine particle material, which is easily lost from the system. This loading of catalyst directly linked to the period of high concentration of fine particles in the emissions stream. It was found that metals, and in particular iron, calcium and silicon form a thick layer on the outside of the catalyst, with large irregular shaped metal ridges, forming along the surface of the particle. These ridges reduce the fluidity of the catalyst, leading to potential disruptions in the regenerator. In addition to this, the metal rich ridges are preferentially removed via attrition, causing metal rich material to be emitted into the atmosphere. To overcome these high particle emissions rates from the FCCU the refinery should only use calcinated catalyst to reduce the influence of thermal process and particle fracture and generation. Although the calcinated catalyst can fracture when added to the system, it is far less than that obtained with uncalicinated catalyst. To further reduce the risk of particle fracture due to thermal stresses the refinery should consider reducing the temperature gradients between the hot and cold catalyst. Due to the economics involved with the regenerator, possible pre-warming of catalyst before addition into system is the preferred option. This pre-heating of catalyst should also incorporate a controlled attrition stage to help remove the build up of metals on the surface of the particles whilst allowing this material to be collected before it can be released into the atmosphere. The remove of the metal crust will also improve the fluidity of the system and reduce the chance of catalyst blockages occurring. Finally, modelling of the system has shown that control of key parameters such as particle size and gas velocity are essential to the management of air emissions. The refinery should look at adjusting start up procedures to remove fluctuations in these key parameters. Also the refinery should be careful in using correlation found in the literature to predicted operational conditions in the system as these correlations are misleading when used under industrial situations.
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Conference papers on the topic "Fluidized Catalytic Cracker Units"

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Sharma, Tanima, Abhishek Sharma, Sourav Verma, and Souryani Mohile. "Sensitivity analysis and grouping of rate constants of aspen kinetic model for a fluidized catalytic cracker." In OIL AND GAS ENGINEERING (OGE-2021). AIP Publishing, 2021. http://dx.doi.org/10.1063/5.0076429.

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Kandassamy, K., E. Natarajan, and S. Renganarayanan. "Producer Gas Cleaning Techniques." In 17th International Conference on Fluidized Bed Combustion. ASMEDC, 2003. http://dx.doi.org/10.1115/fbc2003-061.

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This paper reviews various producer gas cleaning techniques developed/ applied in different biomass gasification processes. It investigates various methods for the removal of particulate matter and tar emissions from producer gas generated by various types of gasifiers. The various tar measurement protocols are inconsistent on the definition of tar and particulate matters. The producer gas if used for power generation using IC engines should be less than 50 mg/Nm3, and in the case of gas turbines a minimum particulate matter concentration of 10 ppm (weight) is needed. To control tars and particulates, various insitu (catalytic tar cracking using Dolomite/Nickel, partial oxidation, high temperature tar cracking, biomass selection, two stage gasification) and post gasification treatments (sand bed filter, wash tower, venturi scrubber, rotational atomizer, electrostatic precipitator, fabric filter, fixed bed tar adsorber, catalytic tar cracker, ceramic filter, cyclones etc) are used. In the cleaning train, collection efficiencies decrease drastically as particulate sizes fall below 1.5 μm. Heavy tar and alkali metals cause engine cylinder deposition and high temperature corrosion of turbine blades respectively. The selection of suitable biomass can improve the quality of gas. Nearly every biomass has a high percentage (60–80%) of Tar Forming Particles (PTFV). Tar is a general nomenclature for a group of compounds like phenols, Poly Aromatic Hydrocarbons (PAH), high Molecular Organic Compounds, Water-soluble organic compounds and ash particles agglomerated with organic compounds. It is easier to remove 90% particulate matter than to achieve 90% tar reduction as they form stable aerosols. A combination of insitu and post gasification treatments is necessary to condition the fuel gas for various power generating equipments. Hence, the analysis of various gas cleaning methods are important for applying them in suitable systems.
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Fraas, Arthur P. "Comparison of Various Fluidized Bed Combustor-Gas Turbine Systems." In ASME 1985 Beijing International Gas Turbine Symposium and Exposition. American Society of Mechanical Engineers, 1985. http://dx.doi.org/10.1115/85-igt-46.

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Pressurizing a fluidized bed combustor with a gas turbine greatly improves both sulfur retention and combustion efficiency. Operating the gas turbine with a high inlet temperature (e.g. 900°C) would yield a thermal efficiency about four points higher than for an atmospheric furnace, but 40 y of experience have failed to solve problems with flyash erosion and deposits. Extensive experience such as that with fluidized bed catalytic cracking units indicates that the gas turbine blade erosion and deposit problems can be handled by dropping the turbine inlet temperature below 400°C where the turbine delivers just enough power to drive the compressor. The resulting thermal efficiency is about half a point higher than for an atmospheric bed, and the capital cost of the FBC-related components is about 40% lower. While a closed-cycle helium gas turbine might be used rather than a steam cycle, the thermal efficiency would be about four points lower and the capital cost of the FBC-related components would be roughly twice that for the corresponding steam plant.
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Cody, G. D., R. J. Bellows, D. J. Goldfarb, H. A. Wolf, and G. V. Storch. "A Novel Non-Intrusive Probe of Particle Motion and Gas Generation in the Feed Injection Zone of the Feed Riser of a Fluidized Bed Catalytic Cracking Unit." In ASME 2000 International Mechanical Engineering Congress and Exposition. American Society of Mechanical Engineers, 2000. http://dx.doi.org/10.1115/imece2000-2047.

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Abstract We define a non-intrusive Acoustic Shot, Noise, ASN, probe of particle velocity at the wall of fluidized beds and transfer lines, and demonstrate how it can be used to obtain quantitative data on changes in particle velocity at the wall through changes in the mean squared wall acceleration of the wall vibrational energy produced by random particle impact or ASN. We note that the probe can be simply calibrated if any two of the following quantities are known for the transfer line: (1) average Axial Velocity of particles; (2) average Axial Mass Density of particles; (3) average Mass Flux of particles. We present the first field data on simultaneous measurements of ASN excited wall vibrational energy along the feed riser of Fluidized Catalytic Cracking Units where catalyst particle flow is produced by the gas generated in the catalytic and thermal cracking of injected oil. We define the Feed Riser Profile as the curve of RMS acceleration along the feed riser and show that changes in its magnitude and shape can be correlated with changes in the product yield of the catalytic and thermal cracking process.
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Tang, Guangwu, Armin Silaen, Bin Wu, Chenn Q. Zhou, Dwight Agnello-Dean, Joseph Wilson, Qingjun Meng, and Samir Khanna. "Numerical Simulation of an Industrial Fluid Catalytic Cracking Regenerator." In ASME 2013 Heat Transfer Summer Conference collocated with the ASME 2013 7th International Conference on Energy Sustainability and the ASME 2013 11th International Conference on Fuel Cell Science, Engineering and Technology. American Society of Mechanical Engineers, 2013. http://dx.doi.org/10.1115/ht2013-17527.

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Fluid catalytic cracking (FCC) is one of the most important conversion processes in petroleum refineries, and FCC regenerator is a key part of an FCC unit to recover the solid catalyst activity by burning off the deposited coke on the catalyst surface. In modern FCC units, regenerator is a cylindrical vessel. Carrier gas transports the solid catalyst from the stripper and feeds the catalyst into the regenerator through catalyst distributors. The catalyst is fluidized by the air that is injected into the regenerator through air rings in the bottom part of the cylindrical vessel. A three-dimensional multi-phase, multi-species reacting flow computational fluid dynamics (CFD) model was established to simulate the flow inside an FCC regenerator. The two phases involved in the flow are gas phase and solid phase. The Euler-Euler approach, where the two phases are considered to be continuous and fully inter-penetrating, is employed. The model includes gas-solid momentum exchange, gas-solid heat exchange, gas-solid mass exchange, and chemical reactions. Chemical reactions incorporated into the model simulate the combustion of coke which is present on the catalyst surface. The simulation results show a good agreement with plant data.
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Treff, Peter, and Craig Johnson. "Clean Power From Coal: Design and Status of East Kentucky Power Cooperative’s E. A. Gilbert Unit." In 18th International Conference on Fluidized Bed Combustion. ASMEDC, 2005. http://dx.doi.org/10.1115/fbc2005-78106.

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East Kentucky Power Cooperative’s (EKPC) E. A. Gilbert unit promises to be one of the cleanest coal fired units in the US. Employing Circulating Fluid Bed (CFB) technology and innovative gas cleaning equipment from ALSTOM, this 268 MW unit will fire a variety of coals. The E. A. Gilbert unit is located at EKPC’s Spurlock Station alongside a 300 MW and a 500 MW pulverized coal unit that were built more than 20 years ago. Low SO2 emissions will be achieved by sulfation of limestone sorbent in the CFB and by additional sulfation of unreacted sorbent in the Flash Dryer AbsorberTM (FDA) system located downstream of the CFB. This will permit low SO2 emissions (0.2 lb/MM BTU, >95% removal). Very low NOx emissions (0.1 lb/MM BTU) are enabled by the low combustion temperatures of the CFB and by the use of selective non-catalytic reduction (SNCR). The latter employs the addition of anhydrous ammonia and extended residence times at low temperature to further reduce NOx within the boiler. Having broken ground in June of 2002, the unit is scheduled to begin firing coal in the winter of 2004–5, with commercial operation scheduled for spring, 2005. Its’ design features and status are the focus of this paper.
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Chang, S. L., B. Golchert, S. A. Lottes, C. Q. Zhou, A. Huntsinger, and M. Petrick. "The Effect of Particle Inlet Conditions on FCC Riser Hydrodynamics and Product Yields." In ASME 1999 International Mechanical Engineering Congress and Exposition. American Society of Mechanical Engineers, 1999. http://dx.doi.org/10.1115/imece1999-1049.

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Abstract Essential to today’s modern refineries and the gasoline production process are fluidized catalytic cracking units. By using a computational fluid dynamics (CFD) code developed at Argonne National Laboratory to simulate the riser, parametric and sensitivity studies were performed to determine the effect of catalyst inlet conditions on the riser hydrodynamics and on the product yields. Simulations were created on the basis of a general riser configuration and operating conditions. The results of this work are indications of riser operating conditions that will maximize specific product yields. The CFD code is a three-dimensional, multiphase, turbulent, reacting flow code with phenomenological models for particle-solid interactions, droplet evaporation, and chemical kinetics. The code has been validated against pressure, particle loading, and product yield measurements. After validation of the code, parametric studies were performed on various parameters such as the injection velocity of the catalyst, the angle of injection, and the particle size distribution. The results indicate that good mixing of the catalyst particles with the oil droplets produces a high degree of cracking in the riser.
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