Somkiat Ngamprasertsith

Coal desulfurization with methanol/water and methanol/KOH

Mae Moh coal from northern Thailand was desulfurized by leaching with methanol/water and methanol/KOH in a batch reactor. The effect of methanol concentration, KOH concentration, coal particles, reaction temperature and reaction time on the removal of ash and sulfur was investigated. Depending on the desulfurization conditions, the reductions ranged from 36 to 74% in pyritic sulfur, 20 to 42% in organic sulfur and 33 to 62% in total sulfur. Methanol/KOH enhanced the desulfurization process in which the inorganic and organic sulfur were removed preferentially. KOH addition can improve the sulfur removal. The kinetics of the oxidation of pyritic sulfur was investigated for Mae Moh coal. The rate of reaction was found to be well represented by a continuous reaction model that was second order with respect to pyritic sulfur.

Biofuel production from palm oil with supercritical alcohols: Effects of the alcohol to oil molar ratios on the biofuel chemical composition and properties

Biofuel production from palm oil with supercritical methanol (SCM) and supercritical ethanol (SCE) at 400 °C and 15 MPa were evaluated. At the optimal alcohol to oil molar ratios of 12:1 and 18:1 for the SCM and SCE processes, respectively, the biofuel samples were synthesized in a 1.2-L reactor and the resulting biofuel was analyzed for the key properties including those for the diesel and biodiesel standard specifications. Biofuel samples derived from both the SCM and SCE processes could be used as an alternative fuel after slight improvement in their acid value and free glycerol content. The remarkable advantages of this novel process were: the additional fuel yield of approximately of 5% and 10% for SCM and SCE, respectively; the lower energy consumption for alcohol preheating, pumping and recovering than the biodiesel production with supercritical alcohols that use a high alcohol to oil molar ratio of 42:1.

Effect of co-solvents on production of biodiesel via transesterification in supercritical methanol

Previous studies on the transesterification of vegetable oil in supercritical methanol in a batch reactor resulted in a non-saponified product with high methyl esters content and high glycerol purity. For the continuous reactor, the high viscosity of vegetable oil might result in problems in the flow system. This study selected THF and hexane as co-solvents to reduce the viscosity of the vegetable oil. The effect of co-solvents was investigated in both 250 mL and 5.5 mL batch reactors by 2-replicate 23 factorial design at temperatures from 290–350 °C, a molar ratio of methanol to vegetable oil from 12–42 and a molar ratio of co-solvent to vegetable oil from 0–5. The reaction time was fixed at 10 min. The products from the employed and unemployed co-solvent process were analyzed by GC-MS to confirm that the reaction among the vegetable oil, methanol and co-solvent was non-existent. However, some thermal cracking was observed in a 250 mL reactor at 350 °C and 30 min reaction time. The amount of co-solvents had no significant effect on methyl esters content and also did not allow the reaction to be completed under milder conditions. Thus, it was concluded that both THF and hexane were appropriate co-solvents to reduce the viscosity of vegetable oil for the continuous production of biodiesel in supercritical methanol.

Biofuel production from crude palm oil with supercritical alcohols: comparative LCA studies.

A recent life cycle assessment (LCA) reported that biodiesel production in supercritical alcohols (SCA) produces a higher environmental load than the homogeneous catalytic process because an enormous amount of energy is required to recover excess alcohol. However, the excess alcohol could be dramatically reduced by increasing the operating temperature to 400°C; although the product would have to be considered as an alternative biofuel instead of biodiesel. A comparative LCA of the biodiesel production in two SCA at 300°C (C-SCA) and novel biofuel production in the same two SCA at 400°C (N-SCA) is presented. It was clear that the N-SCA process produces a dramatically reduced environmental load over that of the C-SCA process due to a lower amount of excess alcohol being used. The N-SCA process could be improved in terms of its environmental impact by changing from fossil fuel to biomass-based fuels for the steam generation.

Supercritical desulfurization of low rank coal with ethanol/KOH

Abstract Desulfurization of Mae Moh coal with supercritical ethanol/potassium hydroxide in a semicontinuous reactor was studied. A two-level factorial experimental design was applied to study the main effects on sulfur reduction. The variables investigated in this work were temperature, pressure, time and potassium hydroxide concentration. The measured responses in the experimental design were coal yield, sulfur reduction and ash reduction. The analysis of the results from the design showed that two variables, temperature and KOH concentration, can be considered to have a significant effect on the pyritic sulfur and total sulfur reduction.

Transesterification in Supercritical Conditions

The transesterification or biodiesel production under supercritical conditions (supercritical transesterification) is a catalyst-free chemical reaction between triglycerides, the major component in vegetable oils and/or animal fats, and low molecular weight alcohols, such as methanol and ethanol, at a temperature and pressure over the critical point of the mixture (see Section 1.1). The overall transesterification reaction is shown in Fig. 1.

Continuous production of biodiesel in supercritical ethanol: a comparative study between refined and used palm olein oils as feedstocks.

Biodiesel production from refined palm olein (RPO) and used palm olein (UPO) oils in supercritical ethanol was comparatively investigated in a continuous reactor. After use of RPO for chicken frying, levels of unsaturated fatty acids (UFAs) and free fatty acid (FFA) increased by 10 and 5%, respectively. The optimal conditions for both oils were 300 °C, 30 MPa and 30:1 ethanol:oil molar ratio at 60 min of residence time. Although the UFAs are inactive and sensitive to thermal degradation, the FFA in UPO catalyzed the reactions in supercritical ethanol at the same time. Due to the antagonistic effect of UFAs and FFA, the maximum ester content of UPO biodiesel (73%) was slightly lower than for RPO biodiesel (80%). The other compounds in resultant biodiesel were unreacted glycerides, mainly mono- and di-glycerides. Furthermore, UPO reaction reached equilibrium faster than RPO reaction due to the catalytic effect of FFA.

Protein and Sugar Extraction from Rice Bran and De-Oiled Rice Bran using Subcritical Water in a Semi-Continuous Reactor: Optimization by Response Surface Methodology

Abstract The extraction of protein and sugar from rice bran and de-oiled rice bran using subcritical water was evaluated in a 30-ml semi-continuous reactor. The effects of the three main factors, operating temperature, time and pressure, on the total sugar and protein yields obtained were investigated using analysis of variance and response surface methodology. A central composite design was performed in order to determine the most likely optimum conditions for the extraction process for both substrates individually and together. The developed models had a very high regression coefficient (R2) value (0.94 – 0.98), and demonstrated that the three main factors investigated had a significant effect on the sugar yield, whilst only time and its interaction with temperature were significant factors controlling the extracted protein yield. Based on the response surface and contour plots, the optimum conditions were evaluated for maximal extracted sugar and protein yields, which reached 100% for protein, from the two materials.

Pretreatment of rice straw by hot-compressed water for enzymatic saccharification

The primary objective of this work was to measure the maximum amount of glucose that can be produced from Thai rice straw using hot-compressed water (HCW)-pretreatment before enzymatic saccharification. The optimal HCW-pretreatment temperature and time were found to be 180 °C/2MPa for 20–30 min. However, the concentrations of the yeast inhibitors were strongly dependent on the HCW-pretreatment temperature and time. At temperatures over 180 °C/2MPa or for more than 30 min at 180 °C/2MPa in the HCW-pretreatment the combined concentration of these two inhibitors (Furfural and 5-Hydroxymethylfurfural) increased exponentially, while the glucose levels were near the maximal asymptote. At the more optimal HCW-pretreatment condition of 180 °C/2MPa for 20 min, 25±3 kg of glucose could be produced from a 100 kg of rice straw, which is potentially economically competitive with other sources

Continuous Production of Biodiesel with Supercritical Methanol: a Simple Compressible Flow Model for Tubular Reactors

From an industrial point of view, the continuous process for biodiesel production with supercritical methanol (SCM) is more appropriate than the batch process. However, lab-scale studies on the continuous process have shown that the maximum conversion always remains slightly lower than that obtained in the batch process. This work proposes a simple compressible flow model to predict the conversion of methanol and oils into methyl esters (ME) along the length of a tubular reactor and further demonstrates the effect of the development of the compressibility factor of the reaction mixture upon the conversion efficiency to ME. The governing equation was derived from a general molar balance in the tubular reactor using transesterification kinetics of refined-bleached-deodorized (RBD) palm oil in SCM coupled with a suitable thermodynamic model with adjusted binary interaction parameters. Vapor-liquid equilibrium data for triolein + methanol, methyl oleate + methanol and glycerol + methanol mixtures were obtained from the literature and then refitted with the thermodynamic model consisting of the Peng-Robinson equation of state and MHV2 mixing rules to find the set of adequate interaction parameters. In order to check the validity of the proposed model, the predicted ME contents were compared with observed values in a lab-scale continuous reactor at various operating temperatures, pressures and methanol to oil molar ratios. The proposed model proved to be adequate for predicting the final conversion to ME for operating temperatures below 320°C, when the thermal degradation reactions of unsaturated fatty acids did not interfere. Our results also illustrate the importance of taking into account the development of the compressibility factor with time and reactor length, since this was shown to be the cause of the lower transesterification reaction rate in the tubular SCM process. The findings in this work could be employed as a knowledgebase to further develop a better model for continuous production of biodiesel with SCM in a tubular reactor.