https://nova.newcastle.edu.au/vital/access/ /manager/Index ${session.getAttribute("locale")} 5 https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:33413 Wed 31 Oct 2018 14:52:21 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:28040 e coal-fired power plant in New South Wales, Australia, for oxy-fuel conversion using integrated chemical looping air separation (ICLAS) technology and cryogenic air separation unit (CASU). The key objectives of this study are to (i) investigate and compare the detailed integration options for oxy-fuel conversion using ICLAS and CASU and (ii) determine the technical merits of the above integration options and the conditions at which the technologies become economically feasible. The study produced scientific evidence that confirms the viability of the CLAS process from both technical and economic points of view under certain conditions. The detailed technical analysis revealed that ICLAS with natural gas integration is energy-efficient compared to CASU running on parasitic load. This is primarily due to the fact that ICLAS needs less auxiliary power compared to CASU. Despite the fact that ICLAS natural gas integration has resulted in higher efficiencies than CASU running on parasitic load, from a series of detailed economic analyses, it was observed that both ICLAS and CASU may not be viable under the present operating and economic conditions. Nevertheless, from sensitivity analysis, it was concluded that ICLAS can become feasible if economic conditions are improved, e.g., a low natural gas market price (<$3.5/GJ), a high electricity wholesale price (>$59/MWh), and/or a high carbon tax (>$33/tonne).]]> Wed 31 Aug 2022 08:48:11 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:47715 Wed 25 Jan 2023 12:12:53 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:38598 Wed 22 Mar 2023 18:40:14 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:43521 Wed 21 Sep 2022 11:25:22 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:50872 50%. Over the range of tested conditions, the critical BSL value was appeared to be insensitive to particle size but increased as Re increased. The diminishing bubble surface mobility is believed to be responsible for the observed trend. Further, a drag modification factor as a function of BSL and Reynolds number has been developed. Noticeably, the drag coefficient curves peaked at the corresponding critical BSL values. The drag modification factor may prove to be useful in modelling of the particle separation processes.]]> Wed 16 Aug 2023 11:05:24 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:51030 Wed 16 Aug 2023 10:16:50 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:49898 Wed 14 Jun 2023 11:18:53 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:37969 Wed 14 Jul 2021 14:33:49 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:47153 i^/) were determined in a solid-liquid fluidised bed comprising glass particles (d_S = 8 mm, ρ_S = 2230 kg m⁻³) and water as a fluidising medium. Both inter-particle and particle-wall collisions were determined from the time varying jerk data. The particle mean-free path (λ) was then estimated as a distance between two successive peaks in the jerk profile. Finally, dispersion efficient D was computed based on the product of λ and V. Estimated dispersion coefficients were compared with the available correlations and reasonable agreement was obtained.]]> Wed 14 Dec 2022 15:34:32 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:27376 Wed 11 Apr 2018 12:37:45 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:12370 Wed 11 Apr 2018 11:10:22 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:13398 Wed 11 Apr 2018 10:18:08 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:46027 3/CaO-CaCl₂. In the charging process of the PCCaL-TES system, surplus energy is stored via sensible heat, latent heat, and chemical energy with the calcination and melting of the solid solution CaCO₃/CaO-CaCl₂. In the discharging process, the carbonation and solidification of CaCO₃/CaO-CaCl₂ takes place and thus the stored energy is retrieved. Compared to the conventional CaL-TES system, the innovative PCCaL-TES system can help maintain a high activity of CaO over long-term operation due to the enhanced heat and mass transfer in the liquid-state carbonation. In this study, the energy storage performance of PCCaL-TES was assessed using the simulation package Aspen Plus v10. According to the modeling results, the PCCaL-TES system can achieve a round-trip efficiency of up to 49% and an energy storage density of nearly 1.5 GJ/m³, presenting improvements of about 4% and 20%, respectively, compared with the conventional CaL-TES system. Meanwhile, a parametric analysis was carried out to examine the effect of key operating parameters on the system performance of PCCaL-TES. The calculations show that the round-trip efficiency of the PCCaL-TES system can be improved by raising the mole fraction of CaCl₂, increasing the carbonator temperature, or employing an optimum carbonator pressure. It was also found that a low mole fraction of CaCl₂, a high activity of CaO, or a low temperature of CO₂ storage was beneficial to achieving a high energy storage density. Finally, the impact of other operating factors on the round-trip efficiency of PCCaL-TES was summarized in a sensitivity analysis. It revealed the round-trip efficiency of the PCCaL-TES system was dominantly determined by the performance of the CO₂ turbine (W-TURB) and compressor (W-COMP), the gas–liquid heat exchanger (HX3) and the exhaust CO₂ cooler (CL3).]]> Wed 09 Nov 2022 15:45:05 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:43917 Wed 05 Oct 2022 09:00:26 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:33986 -1 and 295.8 min^-1 kPa^-1. The same methodology for reaction mechanism determination was carried out for the calcination reaction and G(x)=1-(1-x)^1/3 was found to have the best linear fit. The activation energy and pre-exponential factor determined for the calcination reaction were 103.6 kJ mol^-1 and 6.9 × 10⁶ min^-1, respectively.]]> Wed 04 Sep 2019 12:16:35 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:34169 Tue 31 Mar 2020 15:01:35 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:49593 Tue 23 May 2023 12:03:09 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:51804 Tue 19 Sep 2023 13:56:14 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:47021 Tue 13 Dec 2022 12:44:43 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:34546 Tue 09 Mar 2021 12:01:53 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:46747 Tue 09 Jan 2024 11:43:13 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:40098 Tue 05 Jul 2022 10:34:35 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:27966 Tue 02 Apr 2019 09:36:07 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:31191 −1 cm⁻² and oxygen recovery of 27% at the sintering and operating temperatures of 1200 °C and 900 °C, respectively. At the same operating temperature, under the reducing environment of nitrogen, the LSCF5582 membrane sintered at 1225 °C was found to perform best achieving an oxygen permeation flux and oxygen recovery of 0.77 ml min⁻¹ cm⁻² and 76%, respectively.]]> Tue 01 Oct 2019 13:26:50 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:48426 Thu 16 Mar 2023 14:11:08 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:32961 Thu 16 Aug 2018 14:31:46 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:32959 Thu 16 Aug 2018 13:36:14 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:32956 -3) spherical glass beads particles of diameter 3, 5 and 8 mm and water as fluidising medium with different particle mass ratios varying from 0.17 to 6.0. In the expanded bed, both segregated and intermixed zones were observed depending on the different particle diameter combinations. In a completely segregated SLFB, the bottom monosized layer exhibited a negative deviation ~23% whereas a positive deviation ~25% was found in the top monosized layer when compared with the corresponding pure monosized system. A small mixing zone spanning approximately two particle diameters thick was observed to exist even in a completely segregated SLFB for higher diameter ratio cases. A slight decrease in the mixing zone height was noted with increasing liquid superficial velocity. For lower diameter ratio cases, a relatively lager mixing zone height was observed which increased with increasing liquid superficial velocity. The bed expansion ratio was noted to decrease with increasing solid mass ratio however it increased with increase in the fluidising velocity ratio following a reasonable power law trend. The expanded bed height of the binary mixture was not entirely additive of its corresponding mono-component bed heights and both positive and negative deviations were observed. Finally, a two-dimensional (2D) Eulerian-Eulerian (E-E) model incorporating the kinetic theory of granular flow (KTGF) was used to quantify the binary system hydrodynamics. The model predicted expanded bed height agreed with experimental measurements within ±6% deviation. Presence of a mixing zone was also confirmed by the CFD model and simulated particle phase volume fraction distribution qualitatively agreed with the experimental visualisations.]]> Thu 16 Aug 2018 13:31:39 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:44433 Thu 13 Jul 2023 14:46:58 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:39710 Thu 13 Jul 2023 14:33:29 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:40303 Thu 07 Jul 2022 16:00:38 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:8841 Sat 24 Mar 2018 08:41:16 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:7173 Sat 24 Mar 2018 08:34:18 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:13340 Sat 24 Mar 2018 08:17:00 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:10707 Sat 24 Mar 2018 08:12:14 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:12021 Sat 24 Mar 2018 08:12:08 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:11962 Sat 24 Mar 2018 08:09:35 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20781 Sat 24 Mar 2018 08:05:51 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20522 Sat 24 Mar 2018 08:02:34 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20068 Sat 24 Mar 2018 08:00:12 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20071 Sat 24 Mar 2018 08:00:12 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20072 Sat 24 Mar 2018 08:00:11 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20069 Sat 24 Mar 2018 08:00:11 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20070 Sat 24 Mar 2018 08:00:11 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20888 Sat 24 Mar 2018 07:57:55 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:17144 th of the time required for liquid-liquid mixing in a capillary tube. The rise in the mixing rate was considered to be due to secondary transversal mass transport caused by passive chaotic advection.]]> Sat 24 Mar 2018 07:56:11 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20600 P2/d_P1) and became independent of the foreign particle size for high solid fractions when the fluidised particle size was kept constant. The magnitude of collision force was 10-50 times greater than that of gravitational force and maximally 9 times greater than that of drag force. A correlation describing the collision force as a function of bed voidage was developed for St_p>65 and d_P2/d_P1≤2. A maximum deviation of less than 20% was obtained when the correlation was used for the prediction of particle collision force.]]> Sat 24 Mar 2018 07:55:33 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20979 Sat 24 Mar 2018 07:54:21 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20980 Sat 24 Mar 2018 07:54:20 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:20649 Sat 24 Mar 2018 07:53:09 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:21375 Sat 24 Mar 2018 07:51:27 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:25945 Sat 24 Mar 2018 07:41:26 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:28495 Sat 24 Mar 2018 07:39:32 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:28747 d_PD=5–12 mm) and single air bubbles (d_B=1–4 mm) has been measured in a solid–liquid fluidized bed of uniform size borosilicate glass beads (d_P=5 and 8 mm) as a function of liquid superficial velocity. The homogeneity and intensity of the turbulence within the fluidized bed has been quantified and directly related to the slip velocity of the foreign (steel or bubble) particle. It was found that the turbulence resulted in an increase in the computed drag coefficient for all of the experimental conditions investigated.]]> Sat 24 Mar 2018 07:37:35 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:30699 2 partial pressure (0.05 to 0.1 %), pertinent to a novel greenhouse calcium looping process. The kinetic parameters were obtained and compared with those reported in the literature. Various gas–solid reaction mechanisms were considered to determine the best reaction mechanism for the carbonation reaction. The diffusion function, or G(x)=x², had the best least-squares linear fit, which resulted in a first-order reaction for the carbonation reaction in the greenhouse calcium looping process. Moreover, the activation energy and pre-exponential factor of the carbonation reaction were established to be 19.7 kJ mol⁻¹ and 295.8 min⁻¹ kPa⁻¹, respectively. The derived kinetic parameters were used in Aspen Plus to optimize the carbonator reactor size. The required size of the reactor decreased with increasing operating temperature of the reactor. Exergy analysis revealed that the overall exergetic efficiency of greenhouse calcium looping could be more than 80 %.]]> Sat 24 Mar 2018 07:35:09 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:30334 Sat 24 Mar 2018 07:31:47 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:26057 Sat 24 Mar 2018 07:31:35 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:26078 ex situ tar removal unit, where tar cracking is expected to occur via catalytic reactions with CaO. The current work evaluates the feasibility of the proposed CL-BIGCC concept via thermodynamic analysis using Aspen Plus. Moreover, the tar cracking ability of CaO is demonstrated using thermogravimetric analyzer coupled to Fourier transform infrared spectrometer (TGA-FTIR) experiments. As part of the thermodynamic analysis, sensitivity analyses of the key process parameters, such as the calcium/biomass (Ca/B) ratio, steam/biomass (S/B) ratio, carbonator temperature, and calciner temperature, and their effects on net thermal-to-electricity efficiency have been studied in detail. The optimal values of key process parameters, such as a compression ratio of 5.1, an air/fuel mass ratio of 15, a Ca/B ratio of 0.53, a S/B ratio of 0.17, and carbonator and calciner temperatures of 650 and 800 °C, respectively, have been obtained. Furthermore, the CL-BIGCC process simulated in the current work was found to have a net thermal-to-electricity efficiency of ~25% based on the above optimal parameters, which is the highest among other conventional steam-based BIGCC processes. The biomass gasification (i.e., partial oxidation) experiments in a TGA-FTIR with a CaO/biomass ratio of 1:1 at different temperatures showed that CaO effectively catalyzed tar-cracking reactions.]]> Sat 24 Mar 2018 07:31:31 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:26431 Sat 24 Mar 2018 07:27:29 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:30552 2.5) as it significantly improves the efficiency of conventional particulate removal devices. However, a good understanding of the mechanisms underlying the acoustic agglomeration in the standing wave is largely lacking. In this study, a model that accounts for all of the important particle interactions, e.g., orthokinetic interaction, gravity sedimentation, Brownian diffusion, mutual radiation pressure effect and acoustic wake effect, is developed to investigate the acoustic agglomeration dynamics of PM_2.5 in the standing wave based on the framework of direct simulation Monte Carlo (DSMC) method. The results show that the combination of orthokinetic interaction and gravity sedimentation dominates the acoustic agglomeration process. Compared with Brownian diffusion and the mutual radiation pressure effect, the acoustic wake plays a relatively more important role in governing the particle agglomeration. The phenomenon of particle agglomeration becomes more pronounced when the acoustic frequency and intensity are increased. The model is shown to be capable of accurately predicting the dynamic acoustic agglomeration process in terms of the detailed evolution of particle size and spatial distribution, which in turn allows for the visualization of important features such as “orthokinetic drift”. The prediction results are in good agreement with the experimental data.]]> Sat 24 Mar 2018 07:27:08 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:26647 Sat 24 Mar 2018 07:26:51 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:26045 Sat 24 Mar 2018 07:26:27 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:26545 Sat 24 Mar 2018 07:26:09 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:25528 -3) were used as fluidised particles. Three different combinations of particle size pairs of both equal and unequal mass ratios were used using a constant liquid (water) superficial velocity of 0.17 ms^-1 in all the cases. Numerically, a two dimensional Eulerian-Eulerian (E-E) CFD model incorporating kinetic theory of granular flow (KTGF) was developed to predict the bed expansion behaviour. It was observed that complete bed segregation occurred when the difference between the solid particle diameters was higher while lower difference in particle diameters led to partial bed segregation. The CFD model also predicted these behaviours which were in good agreement with the experimental data.]]> Sat 24 Mar 2018 07:26:07 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:25529 -3 were fluidised in water. Binary experiments were carried out considering both equal and unequal solid mass ratios ranging from 0.16 to 6.0. The overall bed expansions including segregated and intermixed zones were monitored. The effect of loading pattern on bed expansion was found insignificant in a binary SLFB. In a completely segregated SLFB, bottom mono-component layer displayed a negative deviation up to 30% whereas a positive deviation up to 22% was found in top mono-component layer when compared to respective individual monocomponent SLFBs. The total bed height of binary mixture was found to be unequal to sum of expanded bed height in individual mono-component SLFB, showing either positive or negative deviations. The experimentally observed criterion of the bed independency has been tabulated. Eulerian-Eulerian (E-E) CFD simulations with kinetic theory of granular flow (KTGF) have been performed and compared with the experimental data. The CFD predictions were found to be in good agreement (within ±6 per cent deviation) when compared to experimental results.]]> Sat 24 Mar 2018 07:26:07 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:27070 Sat 24 Mar 2018 07:25:19 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:26005 Sat 24 Mar 2018 07:24:35 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:26908 Sat 24 Mar 2018 07:23:35 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:23747 Sat 24 Mar 2018 07:16:57 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:23738 Sat 24 Mar 2018 07:16:55 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:24402 Sat 24 Mar 2018 07:14:27 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:24953 Sat 24 Mar 2018 07:14:18 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:23569 Sat 24 Mar 2018 07:12:46 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:22729 Sat 24 Mar 2018 07:12:25 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:24611 Sat 24 Mar 2018 07:11:55 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:24088 Sat 24 Mar 2018 07:11:46 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:24847 Sat 24 Mar 2018 07:11:24 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:24063 Sat 24 Mar 2018 07:09:41 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:24069 Sat 24 Mar 2018 07:09:39 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:22907 Sat 24 Mar 2018 07:09:32 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:45781 Sat 05 Nov 2022 12:35:15 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:47208 Mon 29 Jan 2024 17:45:48 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:25508 Mon 23 Sep 2019 11:52:21 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:47525 Mon 23 Jan 2023 12:15:50 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:33030 Mon 22 Jun 2020 11:40:21 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:37367 0.1µm and an embryo size smaller than the critical size, otherwise the contribution of direct vapour deposition mechanism could be significant. Based on the scaled nucleation barrier, three distinct nucleation regimes, i.e. athermal heterogeneous nucleation, thermal heterogeneous-dominant nucleation, and homogeneous-dominant nucleation, have been identified. When the contact angle was large, the wetting agent might need to be added to reduce the contact angle so as to reach the athermal heterogeneous and thermal heterogeneous-dominant nucleation regimes, thus achieving efficient particulate abatement at low cost. The prediction results matched reasonably with the experimental data.]]> Mon 19 Oct 2020 14:20:25 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:40737 28.2 °C) the application of the enthalpy-based method leads to erroneous results. For water systems of small volume that often bear a supercooling more than 30 °C, the recalescence stage should be considered in the modelling.]]> Mon 18 Jul 2022 12:58:17 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:37097 Mon 17 Aug 2020 13:30:43 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:34734 0.5Sr_0.5Co_0.8Fe_0.2O_3−δ (LSCF5582) membranes prepared at sintering temperatures of 1200–1300 °C, with the aim of gaining an insight into their performance in the surface reaction limited regime for oxygen separation applications. The findings of this work are then compared with our experimental data on Ba_0.5Sr_0.5Co_0.8Fe_0.2O_3−δ (BSCF5582) membranes. It is demonstrated that the adsorption rate constants of both membranes are two orders of magnitude greater than their respective oxygen desorption rate constants as the oxygen adsorption occurs in less than 24 s whilst the oxygen desorption takes approximately one hour to reach equilibrium. The activation energy for oxygen adsorption of LSCF5582 reduced to a quarter of its value with increasing the sintering temperature from 1200 °C to 1300 °C. This is attributed to the oxygen exchange occurring more rapidly along the grain boundaries resulting in a lower activation energy. The LSCF5582 grain sintered at 1200 °C is the optimum selection for oxygen separation applications at an operating temperature of 850 °C and oxygen partial pressure of 0.21 bar.]]> Fri 31 May 2019 12:54:50 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:29902 2 and CO, attributed to the tar cracking abilities of slag.]]> Fri 31 May 2019 12:33:49 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:40126 Fri 29 Jul 2022 09:16:42 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:45499 Fri 28 Oct 2022 16:00:24 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:45495 Fri 28 Oct 2022 15:53:30 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:43561 Fri 23 Sep 2022 11:36:23 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:37805 Fri 22 Apr 2022 10:22:29 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:35160 th demonstration pilot plant CFM–CLC system (the first of its kind in Australia) that is a scaled-up unit of a lab scale 10-kW_th unit is designed, fabricated and commissioned. The hydrodynamics similarities of the two units in terms of pressure drop profile and solids circulation rate are investigated. The results showed that the scaling factor for the operating velocity calculated based on the dimensionless relation of the fluidisation gas velocity ratio and the square root of the fluidised bed height ratio (of the air reactor) is 2.36, which was in good agreement with the measured value of 2.55. The same solids circulation rate (SCR) between the units was achieved using the scaling factor of 2.55 whilst maintaining the ratio of normalised total solids inventory of the system equal 1. It was also demonstrated that as the ratio of normalised total inventory increased from 1 to 1.4, the gas velocity to achieve similar SCR needs to be reduced proportionally (in the unit which inventory was increased). Therefore, a simple method of calculating the required gas velocity for achieving the same SCR for systems with non-equivalent normalised total solids inventory is proposed. The prediction results using this method were compared against the experimental data, with an average deviation of less than 10%. The validity of the proposed prediction method (for other cases of non-equivalent normalised total solids inventory) however requires further investigation.]]> Fri 21 Jun 2019 15:19:57 AEST ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:37960 S), bubble size (L_B) and rising velocity (V_B) in STFRs and their dependence on operating conditions. Under high Reynolds numbers (Re'≥681), many particles are present in the liquid film and significant bubble surface wave disturbance is observed even when the Capillary number is low (Ca'<0.01). Depending on whether bubble surface distorts (BSD) and/or particles travel between slugs (PTS), four STF patterns are identified and mapped against the flow conditions, with pattern I (with no BSD or PTS) and pattern IV (with both BSD and PTS) occurring at low and high fluids velocities, respectively. The STF patterns are independent of solid loading (when <10%v/v) but show dependency on particle size and flow conditions. Both solid loading and particle size marginally affect V_B, yet have a profound impact on L_B and L_S. Empirical correlations for predicting V_B, L_B and L_S in STFRs are developed. The correlation of V_B proves valid for both slurry and standard Taylor flow systems covering 1.2≤Re'≤3551 and 0.0002≤Ca'≤0.39 for a wide range of fluids in both circular and square channels with size of 480µm-3.02mm.]]> Fri 17 Nov 2023 11:43:25 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:44121 Fri 07 Oct 2022 14:26:45 AEDT ]]> https://nova.newcastle.edu.au/vital/access/ /manager/Repository/uon:49839 Fri 02 Jun 2023 17:06:58 AEST ]]>