Relevant bibliographies by topics / Slurry Reactors

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  1. Journal articles
  2. Dissertations / Theses
  3. Books
  4. Book chapters
  5. Conference papers
  6. Reports

Academic literature on the topic 'Slurry Reactors'

Author: Grafiati
Published: 4 June 2021
Last updated: 17 February 2022

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Journal articles on the topic "Slurry Reactors"

1

Bouchy, M., and O. Zahraa. "Photocatalytic reactors." International Journal of Photoenergy 5, no. 3 (2003): 191–97. http://dx.doi.org/10.1155/s1110662x03000321.

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Fundamental concepts for the design of photocatalytic reactors are recalled: specific rate, modeling of the distribution of the irradiation, description and modeling of transport phenomena on the macroscopic and macroscopic scales. These are required for establishing the reactor mass balance. A brief survey of various reactors is given for solar or artificial light, gas- or liquid-phase, slurry or fixed-bed.
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Tschentscher, Roman, Tjeerd Alexander Nijhuis, John van der Schaaf, and Jaap C. Schouten. "Glucose Oxidation in Slurry Reactors and Rotating Foam Reactors." Industrial & Engineering Chemistry Research 51, no. 4 (2011): 1620–34. http://dx.doi.org/10.1021/ie200694z.

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Bukur, D. B., and W. H. Zimmerman. "Modeling of bubble column slurry reactors for multiple reactions." AIChE Journal 33, no. 7 (1987): 1197–206. http://dx.doi.org/10.1002/aic.690330714.

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4

Ni, Xiong-Wei. "Another Critical Look at Three-Phase Catalysis." Pharmaceutical Fronts 02, no. 03 (2020): e117-e127. http://dx.doi.org/10.1055/s-0040-1722219.

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AbstractThree-phase catalysis, for example, hydrogenation, is a special branch of chemical reactions involving a hydrogen reactant (gas) and a solvent (liquid) in the presence of a metal porous catalyst (solid) to produce a liquid product. Currently, many reactors are being used for three-phase catalysis from packed bed to slurry vessel; the uniqueness for this type of reaction in countless processes is the requirement of transferring gas into liquid, as yet there is not a unified system of quantifying and comparing reactor performances. This article reviews current methodologies in carrying out such heterogeneous catalysis in different reactors and focuses on how to enhance reactor performance from gas transfer perspectives. This article also suggests that the mass transfer rate over energy dissipation may represent a fairer method for comparison of reactor performance accounting for different types/designs of reactors and catalyst structures as well as operating conditions.
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Forret, A., J. M. Schweitzer, T. Gauthier, R. Krishna, and D. Schweich. "Scale Up of Slurry Bubble Reactors." Oil & Gas Science and Technology - Revue de l'IFP 61, no. 3 (2006): 443–58. http://dx.doi.org/10.2516/ogst:2006044a.

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Oinas, Pekka A., and Heikki Haario. "Transient models for multiphase slurry reactors." Catalysis Today 20, no. 3 (1994): 525–39. http://dx.doi.org/10.1016/0920-5861(94)80143-6.

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Wei, Gui, and Hong Chang. "Design of Photocatalytic Reactor with Photocatalyst Film Loaded on Substrate." Advanced Materials Research 823 (October 2013): 214–17. http://dx.doi.org/10.4028/www.scientific.net/amr.823.214.

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After analytical studies of the characteristics of various slurry and supported photocatalytic reactors, a photocatalytic reactor with photocatalyst film loaded on substrate is designed in this paper. This reactor is characterized by the easy attachment and convenient installation & replacement of photocatalyst, higher light utilization, and complete photocatalytic reaction.
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Vlaev, Serafim D., and Jindřich Zahradník. "Energy effectiveness and working characteristics of different tower reactors for aerated slurry systems." Collection of Czechoslovak Chemical Communications 52, no. 11 (1987): 2624–39. http://dx.doi.org/10.1135/cccc19872624.

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Decisive hydrodynamic and mass transfer characteristics of different types of tower reactors (rotating disc reactor, single and multistage sieve-tray bubble columns, tower reactor with ejector gas distributor) as well as the energy effectiveness of their performance were compared with the purpose to establish a quantitative basis for the qualified choice of the proper reactor type according to demands of specific reaction processes. Selected design parameters included gas and solid phase holdup, kLaL, liquid phase residence time distribution, and axial distribution of the solid phase, the experiments were carried out in a wide range of solid phase concentration (0-20 wt. %) and particle sizes (2.3-280 μm). The experimental results proved that due to their favourable suspension characteristics and operation stability the rotating disc reactors can be advantageously used for slow reaction processes with low demands on the intensity of interfacial gas-liquid contact which can be carried out at low gas flow rates. On the other hand the multistage bubble column reactors proved to be superior devices for transport–controlled reaction processes regarding both the achievable rate of interfacial mass transfer and the overall energetic efficiency of phase contacting.
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Rados, Novica, Muthanna H. Al-Dahhan, and Milorad P. Duduković. "Dynamic Modeling of Slurry Bubble Column Reactors." Industrial & Engineering Chemistry Research 44, no. 16 (2005): 6086–94. http://dx.doi.org/10.1021/ie040227t.

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10

Brandi, Rodolfo J., Miguel A. Citroni, Orlando M. Alfano, and Alberto E. Cassano. "Absolute quantum yields in photocatalytic slurry reactors." Chemical Engineering Science 58, no. 3-6 (2003): 979–85. http://dx.doi.org/10.1016/s0009-2509(02)00638-3.

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Dissertations / Theses on the topic "Slurry Reactors"

1

Gopala, Krishna K. V. "Aqueous Phase Oxidation Of Sulfur Dioxide In Stirred Slurry Reactors." Thesis, Indian Institute of Science, 1994. http://hdl.handle.net/2005/130.

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Air pollution by sulfur dioxide is of great concern due to its harmful effects on environment, human beings, fauna and flora. Fossil-fuel-fired power plants are one of the major sources of SO2 emissions. Typically the concentration of SO2 in the flue gases of these plants is in the range of 2000 to 20000 ppm. Flue gas desulfurisation is one of the widely practiced strategies to control SO2 emissions. Aqueous phase oxidation of sulfur dioxide catalysed by carbonaceous particles is an attractive alternative to the conventional processes for flue gas desulfurisation because, amongst other reasons, sulfuric acid, the product of aqueous phase oxidation, finds extensive application in industry. In the literature it has been reported that sulfuric acid affects the solubility of sulfur dioxide and that activated carbon catalyses aqueous phase oxidation. However there is hardly any report on the systematic evaluation of the mechanism of the heterogeneous aqueous phase oxidation of sulfur dioxide which takes into account among other factors, the effect of sulfuric acid on the solubility of SO2 (particularly, at low levels of SO2 and sulfuric acid concentrations). Therefore the objective of the present work is to evaluate systematically the aqueous phase oxidation of SO2 in ppm levels with activated carbon as catalyst in a three-phase agitated slurry reactor and to model rigorously the solubility of SO2 in ppm levels in dilute sulfuric acid solutions and to estimate the concerned parameters experimentally. Strong effect of dilute concentrations of sulfuric acid on the solubility of SO2 is analyzed in terms of the influence of the acid on the equilibrium concentrations of the ionic species (HSO3¯ and SO4¯2 formed from the hydrolysis of SO2 (aq) and the dissociation of H2SO4 respectively) in SO2 - dil. H2SO4 systems. The analysis leads to a general expression relating the partial pressure of SO2 in the gas phase to the concentration of total dissolved SO2 and the concentration of sulfuric acid in the solution. Simple equations are obtained from the general expression for the cases of zero and high concentrations of sulfuric acid in the system, which in turn lead to direct experimental determination of the parameters, Henry's law constant and the equilibrium constant of hydrolysis of SO2 (aq). The developed model predicts the present experimental data as well as the data reported in the literature very closely. The dissolution of SO2, the hydrolysis of SO2 (aq) and the dissociation of H2SO4 are found to be instantaneous. From the dependency of the parameters on temperature, the heat of dissolution of SO2 is determined to be -31.47 kJ mol"1 and the heat of hydrolysis to be 15.69 kJ mol"1. The overall heat of solubility of sulfur dioxide is therefore -15.78 kJ mol"1. Preliminary reaction experiments have clearly indicated that SO2 (aq) does not react and HSO3¯ is the only reactant for aqueous phase oxidation of sulfur dioxide catalysed by activated carbon. The non-reactant SO2 (aq) deactivates the oxidation reaction by competing with HSO3¯ for adsorption on the active sites of the catalyst particles. However the catalyst particles become saturated with SO2 (aq) beyond a certain value of its concentration (saturation limit), which depends on temperature. A mechanism is proposed based on these observations to develop a rate model. The rate model also takes into account the effect of the concentration of the product sulfuric acid on the solubility of sulfur dioxide. The model predicts first order in HSO3¯ , half order in dissolved oxygen and a linear deactivation effect of 5O2(ag). The oxidation reaction is evaluated experimentally at various levels of the operating variables such as temperature and the concentrations of sulfur dioxide and oxygen in the inlet gas. In all experiments a pseudo steady-state region is observed where the gas phase concentration of SO2 reaches a steady value but the concentrations of HSO3¯ and total S (VI) in the liquid phase continue to change. Pseudo steady-state considerations lead to the determination of the initial estimates of the parameters of the rate model namely, the rate constant and the deactivation constant. These parameters are estimated from the transient profiles of the product (sulfuric acid) by solving the model equations by Runge-Kutta method along with Marquardt's non-linear parameter estimation algorithm. The predictions of the model with the estimated parameters match very well with the experimentally observed concentration profiles of S(VI) and HSO3 in the liquid phase and SO2 in the gas phase. The deactivation constant in the saturation range is independent of temperature and is 0.27, which indicates that the intrinsic rate constant is about four times greater than the observed rate constant. From Arrhenius equation-type dependency of the parameters on temperature, the activation energy for the oxidation reaction is determined to be 93.55 kJ mol"1 and for deactivation to be 21.4 kJ mol"1. The low value of activation energy for deactivation suggests a weak dependency of the deactivation on temperature, which perhaps is due to the weak nature of the chemisorption of SO2 (aq) on carbon.
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Yucel, Cakal Gaye O. "Dynamic Behavior Of Continuous Flow Stirred Slurry Reactors In Boric Acid Production." Phd thesis, METU, 2005. http://etd.lib.metu.edu.tr/upload/12605047/index.pdf.

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One of the most important boron minerals, colemanite is reacted with sulfuric acid to produce boric acid. During this reaction, gypsum (calcium sulfate dihydrate) is formed as a byproduct. In this study, the boric acid production was handled both in a batch and four continuously stirred slurry reactors (4-CFSSR&rsquo<br>s) in series system. In this reaction system there are at least three phases, one liquid and two solid phases (colemanite and gypsum). In a batch reactor all the phases have the same operating time (residence time), whereas in a continuous reactor all the phases may have different residence time distributions. The residence time of both the reactant and the product solids are very important because they affect the dissolution conversion of colemanite and the growth of gypsum crystals. The main aim of this study was to investigate the dynamic behavior of continuous flow stirred slurry reactors. By obtaining the residence time distribution of the solid and liquid components, the non-idealities in the reactors can be found. The experiments performed in the continuous flow stirred slurry reactors showed that the reactors to be used during the boric acid production experiments approached an ideal CSTR in the range of the stirring rate (500-750 rpm) studied. The steady state performance of the continuous flow stirred slurry reactors (CFSSR&rsquo<br>s) in series was also studied. During the studies, two colemanites having the same origin but different compositions and particle sizes were used. The boric acid production reaction consists of two simultaneous reactions, dissolution of colemanite and crystallization of gypsum. The dissolution of colemanite and the gypsum formation was followed from the boric acid and calcium ion concentrations, respectively. The effect of initial CaO/ SO42- molar ratio (1.00, 1.37 and 2.17) on the boric acid and calcium ion concentrations were searched. Also, at these initial molar ratios the colemanite feed rate was varied (5, 7.5, 10 and 15 g/min) to change the residence time of the slurry. Purity of the boric acid solution was examined in terms of the selected impurities, which were the magnesium and sulfate ion concentrations. The concentrations of them were compared at the initial molar ratios of 1.00 and 1.37 with varying colemanite feed rates. It was seen that at high initial CaO/ SO42- molar ratios the sulfate and magnesium ion concentrations decreased but the calcium ion concentration increased. The gypsum crystals formed in the reaction are in the shape of thin needles. These crystals, mixed with the insolubles coming from the mineral, are removed from the boric acid slurry by filtration. Filtration of gypsum crystals has an important role in boric acid production reaction because it affects the efficiency, purity and crystallization of boric acid. These crystals must grow to an appropriate size in the reactor. The growth process of gypsum crystals should be synchronized with the dissolution reaction. The effect of solid hold-up (0.04&ndash<br>0.09), defined as the volume of solid to the total volume, on the residence time of gypsum crystals was investigated and the change of the residence time (17-60 min) on the growth of the gypsum was searched. The residence time at each reactor was kept constant in each experiment as the volumes of the reactors were equal. The growth of gypsum was examined by a laser diffraction particle size analyzer and the volume weighted mean diameters of the gypsum crystals were obtained. The views of the crystals were taken under a light microscope. It was observed that the high residence time had a positive effect on the growth of gypsum crystals. The crystals had volume weighted mean diameters of even 240 &micro<br>m. The gypsum crystal growth model was obtained by using the second order crystallization reaction rate equation. The residence time of the continuous reactors are used together with the gypsum growth model to simulate the continuous boric acid reactors with macrofluid and microfluid models. The selected residence times (20-240 min) were modeled for different number of CSTR&rsquo<br>s (1-8) and the PFR. The simulated models were, then verified with the experimental data. The experimentally found calcium ion concentrations checked with the concentrations found from the microfluid model. It was also calculated that the experimental data fitted the microfluid model with a deviation of 4-7%.
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Mthombeni, Bongani. "Modeling Fischer Tropsch synthesis in two-phase, continuous, well-mixed slurry reactors." Master's thesis, University of Cape Town, 2009. http://hdl.handle.net/11427/10853.

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Includes abstract.<br>Includes bibliographical references (p. 84-87).<br>Fischer Tropsch Synthesis (FTS) is the conversion of syngas (CO and H2) to cleaner liquid transportation fuels. The modelling of such a supercritical, highly non-ideal, multi-component system requires the detailed knowledge of the reaction mechanism, reaction kinetics, phase-equilibrium and reactor technology. The objectives of this work were to: develop a complete Fischer Tropsch model, predict the hydrocarbon product distribution, determine what effect Vapour-Liquid Equilibrium (VLE) has on the product distribution, selectivity and kinetics, and determine whether the deviations from the 'ideal' Anderson-Schulz Flory (ASF) distribution can be attributed to VLE.
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Liedtke, Anne-Kathrin. "Study of a new gas-liquid-solid three phase contact mode at millimetric scale : catalytic reactors using “slurry Taylor” flow." Thesis, Lyon 1, 2014. http://www.theses.fr/2014LYO10137/document.

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Des réacteurs avec solide en suspension (« slurry »), très répandu dans l'industrie chimique, du laboratoire à la production, offrent des bonnes capacités en transfert de matière et de chaleur. Leur flexibilité facilite le changement de la phase solide et permet une régénération en continue des catalyseurs en cas de désactivation. Cependant, ils présentent un fort rétro-mélange, et donc un désavantage pour des réactions ayant des enjeux de sélectivité et/ou de conversion poussées. L'écoulement segmenté dit de Taylor est souvent mis en œuvre dans les réacteurs micro-structurés (RMS), grâce à ses propriétés intéressantes (capacités de transfert, écoulement, piston). Cependant, l'utilisation des solides catalytiques dans ces RMS est le plus souvent résolue par immobilisation du catalyseur nuisant la flexibilité. L'écoulement « slurry Taylor » (EST) qui utilise les recirculations internes dans les segments liquides pour transporter des particules en poudre, peut potentiellement répondre à cet enjeu. L'objet de cette étude est la conception et la caractérisation de ce nouveau mode de contact gaz-liquide-solide (G-L-S) dans des tubes millimétriques horizontaux et verticaux. Des études hydrodynamiques ont révélé différents régimes d'écoulement dépendant de la vitesse et de l'orientation de l'écoulement. Pour étudier le transfert de matière L-S, une résine échangeuse d'ion a été utilisée et une première corrélation pour le nombre de Sherwood est proposée<br>Slurry reactors, widely encountered in chemical industry (laboratory scale up to manufactaring), offer good mass and heat transfer capacities and their high flexibility ensures the simple changeover of solid phases enables a continuous online fresh catalyst feed for fast deactivating catalysts. However slurry reactors promote a high degree of backmixing which can be a drawback for reactions with selectivity issues or when very high conversions are required. In microreaction technology, Taylor flow is often employed providing excellent heat and mass transfer and almost ideal plug flow behavior. Solid handing in these small structures is often resolved by immobilizing the solid catalyst which impinges on the flexibility. One possible solution to combine beneficial properties of Taylor flow with the operational flexibility of conventional slurry reactors is a “slurry Taylor” flow (STF) where catalyst particles are suspended and kept in motion by the internal circulations present in the liquid slugs. The focus of this work is the design and characterization of this innovative gas-liquid-solid contactor. Particles were transported in millimetric horizontal and vertical tubing without the risk of clogging. Hydrodynamic studies revealed different flow patterns depending mainly on velocity and flow orientation. Ion exchange resin particles were used to study the liquid-solid mass transfer and first correlation for the Sherwood number in STF is proposed
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Bigg, Torill. "An iron metal slurry reactor for wastewater treatment." Thesis, Cranfield University, 2002. http://dspace.lib.cranfield.ac.uk/handle/1826/11428.

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The corrosion of iron is a very old and complex phenomenon. Its employment for the treatment of wastewater began in the earliest around ten years ago, with few earlier exceptions. Most researchers have considered its application to groundwater remediation, and its use a a permeable reactive barrier material is well established. The aim of this research is to measure parameters that govern zero-valent iron treatment of wastewater with the treatment of industrial influents prior to discharge to municipal sewage treatment works particularly in mind.
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Bigg, T. "In iron metal slurry reactor for wastewater treatment." Thesis, Cranfield University, 2002. http://dspace.lib.cranfield.ac.uk/handle/1826/11428.

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The corrosion of iron is a very old and complex phenomenon. Its employment for the treatment of wastewater began in the earliest around ten years ago, with few earlier exceptions. Most researchers have considered its application to groundwater remediation, and its use a a permeable reactive barrier material is well established. The aim of this research is to measure parameters that govern zero-valent iron treatment of wastewater with the treatment of industrial influents prior to discharge to municipal sewage treatment works particularly in mind.
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Steynberg, Andre Peter. "Process intensification for the iron-catalysed slurry-phase Fischer-Tropsch Reactor System." Master's thesis, University of Cape Town, 2014. http://hdl.handle.net/11427/13279.

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Includes bibliographical references.<br>A set of operating conditions was identified with the potential to enable improved slurryphase reactor productivity for hydrocarbon production using Fischer-Tropsch synthesis. Compared to the most relevant prior art publication, this requires operation at higher gas velocity, higher catalyst concentration and at higher temperature and/or pressure. The closest prior art proposal was published by Van der Laan et al. (1999) and a target was set to improve the reactor productivity by at least 50 %, relative to this reference, while also ensuring stable catalyst performance. Prediction of gas holdup in the reactor is essential to determine the reactor productivity and previous correlations used to predict gas holdup are potentially unreliable for extrapolation to the new proposed conditions. A new approach is adapted, from previous theoretical approaches, to provide a more fundamental and reliable basis for gas holdup prediction. Referred to as the ¡®adapted two-phase theory¡¯ it predicts the gas holdup at any slurry solids concentration using data from a representative solids-free liquid. This approach is shown to provide accurate predictions for paraffinic liquids using data covering a wide range of solids concentrations. Two laboratory reactor experiments were performed, at 260 and 270 ¢ªC, to characterise the selected catalyst performance at conditions relevant to the newly proposed operating regime. An achievable reactor performance was calculated corresponding to the catalyst performance from the experiment at 270 ¢ªC and using the new approach to predict gas holdup. Compared to the proposal by Van der Laan et al. (1999), a reactor with a given diameter is able to produce almost double the amount of product (94 % more with a lower slurry bed height). This is achievable by using higher catalyst concentrations and, most importantly, using a higher operating temperature. The undesirable methane selectivity, at or below 4 %, is still acceptable when operating at 270 ¢ªC. In spite of the higher reactor productivity with increasing temperature, the optimum operating temperature, in the range from 250 to 270 ¢ªC, may depend on the selectivity to the desired hydrocarbon products. The scope for further potential reactor productivity improvement is described. More work is needed to accurately quantify the selected iron catalyst selectivity performance, in the proposed temperature range, but the hydrocarbon selectivity was found to be insensitive to other operating conditions (i.e. pressure and gas composition). It is now possible to better quantify the reactor productivity in the trade-offs which are made with the selectivity performance and the overall plant design configuration which requires recycle of carbon dioxide to the methane reformers to adjust feed gas H2/CO ratio for natural gas applications. The carbon dioxide selectivity for the selected catalyst at the conditions tested was found to be too high for gas-to-liquid (GTL) applications using a natural gas feed.
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Lamaignère, Valérie. "Effects of hydrodynamic stress on growing Saccharomyces cerevisiae in a slurry reactor." Master's thesis, University of Cape Town, 2003. http://hdl.handle.net/11427/6081.

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Includes bibliography.<br>The objectives of this research thesis were to understand and quantify biological responses to hydrodynamic stress by investigating the activity of the yeast Saccharomyces cerevisiae, cultivated in the presence of a range of solid loadings, solid sizes and agitation rates. The influence of inoculum size, inoculum age and type of agitator were also investigated. This study was carried out with the intention of identifying biological responses to hydrodynamic stress and modelling observed effects on microbial activity.
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Peña, Zapata Diego. "Identification of deactivation mechanisms of cobalt Fischer-Tropsch catalysts in slurry reactor." Thesis, Lille 1, 2013. http://www.theses.fr/2013LIL10149/document.

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La synthèse Fischer -Tropsch (SFT) produit des carburants liquides ultra-propres, ainsi que des produits chimiques à partir du gaz de synthèse issu d’une large gamme de matières premières : gaz naturel, gaz de schiste, charbon, biomasse. Les catalyseurs supportés à base de cobalt sont la meilleure option pour la SFT à basse température, en raison de leur grande stabilité et leur sélectivité en hydrocarbures lourds. Néanmoins, ces catalyseurs se désactivent avec le temps au cours de la réaction. La désactivation réduit la durée de vie et la productivité de ces catalyseurs. Par conséquent, la désactivation reste un défi majeur de la SFT. Dans ce travail, nous avons identifié les mécanismes les plus pertinents de la désactivation du catalyseur à base de cobalt dans le réacteur slurry : frittage du cobalt, attrition du catalyseur et dépôt de carbone. Il est démontré que la vitesse de désactivation dépend des conditions opératoires. Les résultats expérimentaux suggèrent que l'attrition du catalyseur est fortement influencée par la pression partielle d’eau dans le réacteur. La pression partielle élevée d’eau favorise la mobilité des nanoparticules de cobalt à la surface et leur frittage. Des agglomérats de cobalt de quelques microns situés sur des grains de catalyseur, ainsi que des particules métalliques de cobalt individuelles ont été observés dans les catalyseurs usés. La formation des agglomérats de cobalt a été favorisée à des vitesses spatiales basses et dans le gaz de synthèse pauvre en hydrogène. La dilution du gaz de synthèse au début de la réaction diminue l’attrition et réduit la formation des agglomérats de cobalt. Des hydrocarbures, des alcools, des cétones, des aldéhydes, des acides organiques ont été détectés dans les catalyseurs usés ; α -oléfines étant les espèces les plus abondantes. Les acides carboxyliques et les aldéhydes cinnamiques semblent être le plus néfastes pour les performances catalytiques. Le schéma de la formation de différentes espèces de carbone à la surface des catalyseurs de cobalt dans le réacteur slurry été proposé dans le manuscrit<br>The Fischer-Tropsch Synthesis (FTS) produces ultra-clean liquid fuels and chemicals via conversion of syngas from a wide range of feedstocks: natural gas, shale gas coal and biomass. Supported cobalt-based catalysts are the best option for the low temperature FTS, due to their high stability and selectivity toward heavy paraffinic hydrocarbons. Nevertheless, cobalt catalysts deactivate with time on stream. This leads to a decrease in catalyst lifetime and productivity. Hence, catalyst deactivation remains a major challenge of FTS. In this work we identified cobalt sintering, catalyst attrition and carbon deposition as the most relevant catalyst deactivation mechanisms in slurry reactor; the deactivation rate being influenced by the operating conditions. The experimental results suggest that catalyst attrition is strongly affected by water partial pressure in the catalytic reactor. High water partial pressure favours mobility of cobalt nanoparticles on surface and cobalt sintering. Both cobalt agglomerates of micron size located on catalyst grains and detached cobalt metal particles were observed in the spent catalysts. The formation of cobalt agglomerates was favoured at lower gas space velocity and in H2-deficient syngas. Syngas dilution at the beginning of reaction decreases the degree of attrition and reduces cobalt agglomerate formation. Hydrocarbons, alcohols, ketones, aldehydes, organic acids were detected in the spent catalysts; α-olefins being the most abundant species. Carboxylic acids and alpha-alkyl cinnamic aldehyde seem to be most detrimental for the catalytic performance. A tentative schema of formation of different carbon species in cobalt catalysts during FTS in slurry reactor has been proposed in the manuscript
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Inga, Juan Ricardo. "Hydrodynamic studies and reactor modelling of a three phase slurry reactor in Fischer Tropsch application / Juan Ricardo Inga." Thesis, Potchefstroom University for Christian Higher Education, 1992. http://hdl.handle.net/10394/9611.

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In this .study the hydrodynamic characteristics of the slurry bed reactor was investigated. This study was aimed to the under" standing of the important parameters that describe the hydrodynamic regime and their quantification. In order to determine the relevant parameters the use of a theoretical model was necessary. This model should include all the hydrodynamic parameters in form of correlations. A sensitivity study was done and the parameters which have great impact were determined. An extensive literature review was done in order to gather the experience of previous investigations. Unfortunately all the experience was obtained in a different hydrodynamic regime and therefore the published results could not be used directly in our study. Hydrodynamic test were performed in the works pilot plant at the operating conditions. Unlike a laboratory, the instrumentation used was the one use in commercial reactors with the commercially acceptable range of accuracy. A mass balance was done around the reactor to ensure that the data was sound. Heat balance was also performed and the study of the heat transfer coefficient was performed. Although this was beyond the scope of this study was here included due to its importance in the design of slurry bed reactors. An existing computer model was adapted for the churn-turbulent regime and the hydrodynamic parameters were implemented. This reactor model was coupled with flashes subroutines in order to have a complete reactor train. This computer model was used for the design of the Slurry Bed Commercial Reactor to be commissioned on 1993 at Sasol One.<br>Thesis (MIng (Chemies))--PU for CHE, 1993
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Books on the topic "Slurry Reactors"

1

Polymerisation of ethylene: In slurry loop reactors. Walter de Gruyter GmbH & Co., KG, 2015.

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Vinke, Heinz. The effect of catalyst particle-to-bubble adhesion on the mass transfer in agitated slurry reactors. s.n.], 1992.

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Stangle, Gregory Charles. Mass transfer with chemical reaction in a three-phase foam slurry reactor. 1985.

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Superfund Innovative Technology Evaluation Program (U.S.), ed. Pilot-scale demonstration of a slurry-phase biological reactor for creosote-contaminated soil. U.S. Environmental Protection Agency, Superfund Innovative Technology Evaluation, 1993.

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Superfund Innovative Technology Evaluation Program (U.S.), ed. Pilot-scale demonstration of a slurry-phase biological reactor for creosote-contaminated soil. U.S. Environmental Protection Agency, Superfund Innovative Technology Evaluation, 1993.

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Superfund Innovative Technology Evaluation Program (U.S.), ed. Pilot-scale demonstration of a slurry-phase biological reactor for creosote-contaminated soil. U.S. Environmental Protection Agency, Superfund Innovative Technology Evaluation, 1993.

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Pilot-scale demonstration of a slurry-phase biological reactor for creosote-contaminated soil. U.S. Environmental Protection Agency, Superfund Innovative Technology Evaluation, 1993.

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Majid, Dosani, and Risk Reduction Engineering Laboratory (U.S.), eds. On-site engineering report of the slurry-phase biological reactor for pilot-scale testing on contaminated soil: Project summary. Risk Reduction Engineering Laboratory, U.S. Environmental Protection Agency, 1993.

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Majid, Dosani, and Risk Reduction Engineering Laboratory (U.S.), eds. On-site engineering report of the slurry-phase biological reactor for pilot-scale testing on contaminated soil: Project summary. Risk Reduction Engineering Laboratory, U.S. Environmental Protection Agency, 1993.

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Majid, Dosani, and Risk Reduction Engineering Laboratory (U.S.), eds. On-site engineering report of the slurry-phase biological reactor for pilot-scale testing on contaminated soil: Project summary. Risk Reduction Engineering Laboratory, U.S. Environmental Protection Agency, 1993.

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Book chapters on the topic "Slurry Reactors"

1

Buwa, Vivek V., Shantanu Roy, and Vivek V. Ranade. "Three-phase slurry reactors." In Multiphase Catalytic Reactors. John Wiley & Sons, Inc., 2016. http://dx.doi.org/10.1002/9781119248491.ch6.

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Beenackers, A. A. C. M., and W. P. M. Swaaij. "Slurry Reactors, Fundamentals and Applications." In Chemical Reactor Design and Technology. Springer Netherlands, 1986. http://dx.doi.org/10.1007/978-94-009-4400-8_13.

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Doğu, Gülşen, Gökhan Ölmez, and Timur Doğu. "Removal of SO2 with Lime Slurry in a Spray Dryer." In Chemical Reactor Technology for Environmentally Safe Reactors and Products. Springer Netherlands, 1992. http://dx.doi.org/10.1007/978-94-011-2747-9_20.

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Arastoopour, Hamid, Dimitri Gidaspow, and Robert W. Lyczkowski. "Synthetic Gas Conversion to Liquid Fuel Using Slurry Bubble Column Reactors." In Mechanical Engineering Series. Springer International Publishing, 2021. http://dx.doi.org/10.1007/978-3-030-68578-2_6.

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Nocentini, M., and F. Magelli. "Solid Distribution in Slurry Reactors Stirred with Multiple Impellers: Continuous Flow Systems." In Fluid Mechanics and Its Applications. Springer Netherlands, 1992. http://dx.doi.org/10.1007/978-94-015-7973-5_9.

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Alfano, Orlando M., Alberto E. Cassano, Rodolfo J. Brandi, and María L. Satuf. "A Methodology for Modeling Slurry Photocatalytic Reactors for Degradation of an Organic Pollutant in Water." In Photocatalysis and Water Purification. Wiley-VCH Verlag GmbH & Co. KGaA, 2013. http://dx.doi.org/10.1002/9783527645404.ch13.

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Gamwo, Isaac K., Dimitri Gidaspow, and Jonghwun Jung. "Slurry Bubble Column Reactor Optimization." In ACS Symposium Series. American Chemical Society, 2007. http://dx.doi.org/10.1021/bk-2007-0959.ch017.

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Böhm, L. L. "The Slurry Polymerization Process with Super-Active Ziegler-Type Catalyst Systems: From the 2 L Glass Autoclave to the 200 m3 Stirred Tank Reactor." In Polyolefins: 50 years after Ziegler and Natta I. Springer Berlin Heidelberg, 2013. http://dx.doi.org/10.1007/12_2013_214.

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Vogela, Alex, Andre Steynberg, and Berthold Breman. "Intensification of commercial slurry phase reactors." In Studies in Surface Science and Catalysis. Elsevier, 2007. http://dx.doi.org/10.1016/s0167-2991(07)80109-1.

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Doraiswamy, L. K. "Multiphase Reactions and Reactors." In Organic Synthesis Engineering. Oxford University Press, 2001. http://dx.doi.org/10.1093/oso/9780195096897.003.0025.

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The first three chapters of this part dealt with two-phase reactions. Although catalysts are not generally present in these systems, they can be used in dissolved form in the liquid phase. This, however, does not increase the number of phases. On the other hand, there are innumerable instances of gas-liquid reactions in which the catalyst is present in solid form. A popular example of this is the slurry reactor so extensively employed in reactions such as hydrogenation and oxidation. There are also situations where the solid is a reactant or where a phasetransfer catalyst is immobilized on a solid support that gives rise to a third phase. A broad classification of three-phase reactions and reactors is presented in Table 17.1 (not all of which are considered here). This is not a complete classification, but it includes most of the important (and potentially important) types of reactions and reactors. The thrust of this chapter is on reactions and reactors involving a gas phase, a liquid phase, and a solid phase which can be either a catalyst (but not a phasetransfer catalyst) or a reactant, with greater emphasis on the former. The book by Ramachandran and Chaudhari (1983) on three-phase catalytic reactions is particularly valuable. Other books and reviews include those of Shah (1979), Chaudhari and Ramachandran (1980), Villermaux (1981), Shah et al. (1982), Hofmann (1983), Crine and L’Homme (1983), Doraiswamy and Sharma (1984), Tarmy et al. (1984), Shah and Deckwer (1985), Chaudhari and Shah (1986), Kohler (1986), Chaudhari et al. (1986), Hanika and Stanek (1986), Joshi et al. (1988), Concordia (1990), Mills et al. (1992), Beenackers and Van Swaaij (1993), and Mills and Chaudhari (1997). Doraiswamy and Sharma (1984) also present a discussion of gas-liquid-solid noncatalytic reactions in which the solid is a reactant. In Chapter 7 we saw how Langmuir-Hinshelwood-Hougen-Watson (LHHW) models are normally used to describe the kinetics of gas-solid (catalytic) or liquid-solid (catalytic) reactions, and in Chapters 14 to 16 we saw how mass transfer between gas and liquid phases can significantly alter the rates and regimes of these two-phase reactions.
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Conference papers on the topic "Slurry Reactors"

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Ahsan, Syed Saad, and David Erickson. "Microfluidic Photocatalytic Water-Splitting Reactors." In ASME 2012 International Mechanical Engineering Congress and Exposition. American Society of Mechanical Engineers, 2012. http://dx.doi.org/10.1115/imece2012-87860.

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In this work, we present a novel microfluidic photocatalytic water-splitting reactor. Optofluidics offers advantages over conventional reactors in terms of improved photon transfer efficiency and mass transfer efficiency and are therefore the ideal platform for photocatalytic reactions. Our device is a planar optofluidic device which we used to study the kinetics of Platinum-Impregnated Titanium Oxide as the oxygen and hydrogen producing photocatalyst redox mediated by Iodide/Iodate species. We deposit our catalysts via a sol-gel method while the platinum co-catalyst is added by wet impregnation via reduction in Sodium Borohydride. The reactions are performed under a 100W Hg lamp and reaction rates are inferred by measuring the depletion of the two Iodine species via UV-vis absorption spectrophotometry. Our results indicate that reaction rates and efficiencies can be enhanced by using an optofluidic platform as opposed to the conventional slurry reactor used in previous experiments for this class of reaction. We believe that the micro-optofluidic platform of our device offers the benefit of measuring the kinetic properties of these class of reactions quickly and cheaply for the goals of further optimization.
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Chen, Haiying, Aizhong Ding, Junfeng Dou, et al. "Optimal Conditions for Biodegradation of Indeno (1,2,3-cd) Pyrene in Soil Slurry Reactors." In 2010 4th International Conference on Bioinformatics and Biomedical Engineering (iCBBE). IEEE, 2010. http://dx.doi.org/10.1109/icbbe.2010.5517395.

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Pasangulapati, V., N. R. Kesana, G. Sharma, F. W. Chambers, M. E. McNally, and R. M. Hoffman. "Computational Study of Slurry Flow in Pipes to Determine Profiles Sensed in Near Infrared Slurry Measurements." In ASME 2011 International Mechanical Engineering Congress and Exposition. ASMEDC, 2011. http://dx.doi.org/10.1115/imece2011-62799.

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It is desired to perform accurate Near Infrared sensor measurements of slurries flowing in pipes leaving large batch reactors. A concern with these measurements is the degree to which the slurry sensed is representative of the material in the reactor and flowing through the pipe. Computational Fluid Dynamics (CFD) has been applied to the flow in the pipe to determine the flow fields and the concentration profiles seen by the sensors. The slurry was comprised of a xylene liquid phase and an ADP (2-amino-4, 6-dimethylpyrimidine) solid phase with a density ratio of 1.7. Computations were performed for a horizontal pipe with diameter 50.8 mm, length 2.032 m, and 1.76 m/s and 3.26 m/s mixture velocities. The corresponding pipe Reynolds numbers were 1.19E+05 and 2.21E+05. The flow through a slotted cylindrical probe inserted radially in the pipe also was considered. Spherical slurry particles with diameters from 10 μm to 1000 μm were considered with solid volume fractions of 12%, 24%, and 35%. Computations were performed with ANSYS FLUENT 12 software using the Realizable k-ε turbulence model and the enhanced wall treatment function. Comparisons of computed vertical profiles of solid volume fraction to results in the literature showed good agreement. Symmetric, nearly flat solid volume fraction profiles were observed for 38 μm particles for all three initial solid volume fractions. Asymmetric solid volume fraction profiles with greater values toward the bottom were observed for the larger particles. Changes in the profiles of turbulent kinetic energy also were observed. These changes are important for optical measurements which depend upon the mean concentration profiles as well as the turbulent motion of the slurry particles.
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Torabifar, B., A. Torabian, A. A. Azimi, and M. Vossoughi. "Biological treatment of petroleum contaminated soils by soil slurry-sequencing batch reactors (SS-SBRs)." In WASTE MANAGEMENT 2008. WIT Press, 2008. http://dx.doi.org/10.2495/wm080761.

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Ademola O ADEBAYO, Simeon O JEKAYINFA, and Bernd LINKE. "Biogas Potential of Cow Slurry in Continuously Stirred Tank Reactors at Mesophilic and Thermophilic Temperatures." In 2012 Dallas, Texas, July 29 - August 1, 2012. American Society of Agricultural and Biological Engineers, 2012. http://dx.doi.org/10.13031/2013.41922.

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Kritzinger, H. P., B. C. Deelder, C. R. Kleijn, J. J. Derksen, and H. E. A. Van den Akker. "Turbulent Flow in a Stirred Tank With Permeable Impeller Blades." In ASME 2002 Joint U.S.-European Fluids Engineering Division Conference. ASMEDC, 2002. http://dx.doi.org/10.1115/fedsm2002-31360.

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This paper presents results from the experimental investigation of single-phase flow in a prototype stirred tank reactor, which uses monolith catalyst blocks as impeller. These monolith catalyst supports have been used for a dual role: (i) as stirrer blades for agitation and (ii) to bring reactants in contact with the catalyst in a way that eliminates the need for product filtration. The reactors are under investigation as replacement for the standard slurry stirred tank reactors used in the catalytic processes in chemical industry. The flow field in the reactor with this novel impeller, was determined using LDA. Mean and fluctuating velocity data were measured for different monolith blocks and impeller speeds. Results show the normalized flow in the bulk of the tank to be independent of impeller speed and monolith type. Flow velocities through the monolith channels, which are crucial to bring the reactants in contact with the catalyst impregnated in the monolith walls, were measured with LDA. These velocities were found to be of the order of 30–70% of the impeller tip velocity, dependent on the impeller speed and monolith type.
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Kostedt, William L., Mickal A. Witwer, David W. Mazyck, Tony Powell, and Brian Butters. "A Slurry-Based Photocatalytic Reactor with Slurry Separation for Water Recovery." In International Conference On Environmental Systems. SAE International, 2005. http://dx.doi.org/10.4271/2005-01-2994.

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Ahmadi, Goodarz, and Xinyu Zhang. "Gas-Liquid-Particle Three-Phase Flows in Bubble Columns." In ASME/JSME 2003 4th Joint Fluids Summer Engineering Conference. ASMEDC, 2003. http://dx.doi.org/10.1115/fedsm2003-45556.

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An Eulerian-Lagrangian computational model for simulations of gas-liquid-solid flows in three-phase slurry reactors is developed. In this approach, the liquid flow is modeled using a volume-averaged system of governing equations, whereas motions of bubbles and particles are evaluated by Lagrangian trajectory analysis procedure. It is assumed that the bubbles remain spherical and their shape variations are neglected. The two-way interactions between bubble-liquid and particle-liquid are included in the analysis. The discrete phase equations include drag, lift, buoyancy, and virtual mass forces. Particle-particle interactions are accounted for by the hard sphere model approach. The bubble collisions and coalescence are also included in the computational model. The simulation results show that the transient characteristics of the three-phase flow in a column are dominated by time-dependent staggered vortices. The bubble plume moves along a S-shape path and exhibit an oscillatory behavior. While most particles are located outside the vortices, some bubbles and particles are retained in the vortices. Bubble upward velocities are much larger than both liquid and particle velocities. Particle upward velocities are slightly smaller than the liquid velocities.
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Nwaigwe, Kevin N., Nnamdi V. Ogueke, Chibuike Ononogbo, and Emmanuel E. Anyanwu. "Performance Study of Anaerobic Digestion of Organic Municipal Waste in Upflow Bioreactor With Central Substrate Dispenser." In ASME 2013 International Mechanical Engineering Congress and Exposition. American Society of Mechanical Engineers, 2013. http://dx.doi.org/10.1115/imece2013-64064.

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A performance study of anaerobic digestion of organic municipal waste in upflow bioreactor with central substrate dispenser is presented. The experimental rig is based on an integrated system of bioreactors consisting of Upflow Bioreactor (UB), Upflow Bioreactor with Central Subtrate Dispenser (UBCSD), and Continous Stirred Tank Reactor (CSTR) each having internal volume of 76 litres, 64.8 litres, and 76 litres respectively. The scheme is used for minimizing the mixing and fouling problems associated with some conventional bioreactors during digestion reaction. Organic municipal waste (OMW) was used to prepare the slurry for the reactors. Microbial reaction was enhanced during operation using a measured quantity (2kg) of substances from the rumen of a newly slaughtered cow. The experimentation from feeder tank to Bioreactors was carried out for a period of 10-days Hydraulic Retention Time (HRT) at 37°C. Effects of some basic parameters affecting anaerobic digestion in terms of biogas production and Chemical Oxygen Demand (COD) reduction were carried out. They include substrate temperature, minimal average temperature, changes in temperature, substrate content and properties, available nutrient, retention time, organic loading rate, pH level, nitrogen inhibition and C/N ratio, substrate agitation, and inhibitory factors. Results showed that UBSCD generated the highest level of Biogas yield of up to 52915 ml, while UB and CSTR yielded 23550ml and 28980ml respectively. Similarly for COD removal, 24343 mg/l, 5775.4 mg/l, and 23155 mg/l were achieved for UBCSD, UB and CSTR respectively from an initial value of 120,320 mg/l. These results show that the use of UBCSD better enhances biofuel production from organic municipal waste.
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Strasser, W., and A. Wonders. "Commercial scale slurry bubble column reactor optimization." In ADVANCES IN FLUID MECHANICS 2008. WIT Press, 2008. http://dx.doi.org/10.2495/afm080271.

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Reports on the topic "Slurry Reactors"

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Andrew Lucero. Improved Fischer-Tropsch Slurry Reactors. Office of Scientific and Technical Information (OSTI), 2009. http://dx.doi.org/10.2172/993519.

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Clark, N., J. Kuhlman, I. Celik, R. Gross, E. Nebiolo, and Yi-Zun Wang. Circulation in gas-slurry column reactors. Office of Scientific and Technical Information (OSTI), 1990. http://dx.doi.org/10.2172/6472190.

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Clark, N., J. Kuhlman, and I. Celik. Circulation in gas-slurry column reactors. Office of Scientific and Technical Information (OSTI), 1989. http://dx.doi.org/10.2172/5419261.

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Dimitri Gidaspow. Hydrodynamic models for slurry bubble column reactors. Office of Scientific and Technical Information (OSTI), 1996. http://dx.doi.org/10.2172/750375.

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Goodarz Ahmadi. ADVANCED COMPUTATIONAL MODEL FOR THREE-PHASE SLURRY REACTORS. Office of Scientific and Technical Information (OSTI), 2000. http://dx.doi.org/10.2172/825379.

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Goodarz Ahmadi. ADVANCED COMPUTATIONAL MODEL FOR THREE-PHASE SLURRY REACTORS. Office of Scientific and Technical Information (OSTI), 2001. http://dx.doi.org/10.2172/825380.

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Goodarz Ahmadi. ADVANCED COMPUTATIONAL MODEL FOR THREE-PHASE SLURRY REACTORS. Office of Scientific and Technical Information (OSTI), 2004. http://dx.doi.org/10.2172/838723.

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Paul Lam and Dimitri Gidaspow. COMPUTATIONAL AND EXPERIMENTAL MODELING OF SLURRY BUBBLE COLUMN REACTORS. Office of Scientific and Technical Information (OSTI), 2000. http://dx.doi.org/10.2172/825383.

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Paul Lam and Dimitri Gidaspow. COMPUTATIONAL AND EXPERIMENTAL MODELING OF SLURRY BUBBLE COLUMN REACTORS. Office of Scientific and Technical Information (OSTI), 2001. http://dx.doi.org/10.2172/825384.

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Paul C.K. Lam, Isaac K. Gamwo, and Dimitri Gidaspow. COMPUTATIONAL AND EXPERIMENTAL MODELING OF SLURRY BUBBLE COLUMN REACTORS. Office of Scientific and Technical Information (OSTI), 2002. http://dx.doi.org/10.2172/825795.

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