Model test set up methodology for HDS to improve the understanding of reaction pathways in HDT catalysts
|
|
- Silvia Sabina Jennings
- 5 years ago
- Views:
Transcription
1 Model test set up methodology for HDS to improve the understanding of reaction pathways in HDT catalysts Paulo, D. 1,2, Guichard, B. 2, Delattre, V. 2, Lett, N. 2, Lemos, F. 1 1 Instituto Superior Técnico, Chemical and Biological Engineering Department, Lisbon, Portugal. 2 Institut Français du Pétrole Énergies nouvelles, Catalysis and Separation Division, Catalysis by Sulfides Department, Solaize, France. Abstract In this present work, the hydrodesulfurization (HDS) of 4,6-dimethyldibenzothiophene (4,6-DMDBT) was studied over three CoMo/Al 2 O 3 catalysts (dried, calcined and additive impregnated) in a fixed-bed reactor under standard conditions close to those usually used in diesel fuel hydrotreating following particularly the HYD and DDS pathways behaviors. The main focus was to identify some strong differences in behavior between the various catalysts and evaluate the effect of H 2 S, NH 3 and H 2 partial pressures on their relative catalytic performances. It was found by experimental and modelling results that, at standard conditions, the additive impregnated catalyst performs better and was less impacted by H 2 S adsorption than dried and calcined. Though, in the presence of high amounts of H 2 S, the additive impregnated showed to be the one differing mostly from H 2 S partial pressure. In addition, the study on the impact of nitrogen-based compounds (quinoline) revealed that all three catalysts are similar inhibited. In the same way, modifying the partial pressure of H 2 was found to enhance the activity of all catalysts, especially the HYD pathway. A more detailed study and additional experimental tests should be performed in order to improve the understanding on the relation between quinoline and H 2 S within the deep HDS of 4,6-DMDBT and to further develop the kinetic model created. Keywords: Diesel; middle distillates; 4,6-DMDBT; CoMo/Al 2 O 3 ; inhibition effect. 1 Introduction In order to decrease pollution caused by automobile vehicles, the sulfur content in diesel fuel has been drastically reduced over the years as witnesses the restrictive regulations. However, refining industries are processing heavier feedstocks and facing an increasing demand on fuels so, a better performance from the hydrodesulfurization (HDS) catalysts is required. The commercial catalysts commonly used for HDS reactions are molybdenum sulfides promoted by cobalt or nickel and supported over alumina. Nevertheless, if one aims to improve their performances, it is now necessary to identify precisely the limitations. It can be achieved by characterizing deeply the catalyst, using powerful tools or by carrying a kinetic study to identify the main limitation, inhibiting and activating parameters. To do so, it is necessary to evaluate the catalyst in representative conditions witnessing the way it will have to work in real conditions. In the HDS of middle distillates, as sulfur conversion increases the remaining species are mostly dibenzothiophenes. As 4,6-DMDBT, these compounds are very difficult to decompose. Moreover, these compounds are decomposed through two main and distinct pathways namely, hydrogenation (HYD) and direct desulfurization (DDS). Furthermore, the presence of the methyl groups on 4,6-DMDBT highly limits the reactivity and leads the HDS to selectively process through the hydrogenating route compared to the DDS one. The objective of this work was focused on the comprehension of the HDS mechanism on various representatives CoMo catalyst types in order to study the deep HDS of middle distillates in the range of operating conditions dedicated to the low pressure HDS. 1
2 2 Methodology 2.1 Catalysts Three types of catalysts were prepared CoMo-A, CoMo-B and CoMo-C. All used catalysts are CoMo trilobe extrudates supported on γ-alumina. In order to process to their catalytic evaluation, their length has been calibrated between 2 and 4 mm for hydrodynamic considerations. These catalysts were prepared by three common stages: active phase impregnation (dry impregnation), maturation (in air atmosphere for 1,5 hours) and drying (at 90 C for 24 hours). CoMo-A was the only catalyst used directly on the catalytic tests after drying phase. CoMo-B was calcined under air at 450 C, for 120 minutes, and to produce CoMo-C catalyst, an organic solution was added as an additive, at pore volume, which was then dried under nitrogen flow at 140 C and two hours to preserve the organic compound but eliminating the solvent. The catalysts samples (4 cm 3 ) were loaded with silicon carbide in the reactor to ensure good thermal diffusion in the catalyst bed. They were sulfided in situ in the reactor using a sulfidation feedstock containing DMDS, xylene and cyclohexane. This mixture was injected at a starting temperature of 40ºC. After 3h, the temperature was raised to 350ºC at a 1,7ºC/min rate and was maintained at 350ºC for 1h, before decreasing to 290ºC at a 1,5ºC/min. 2.2 Reaction Conditions For this study, the HDS of 4,6-DMDBT was carried out in a high-pressure fixed-bed microreactor (length: 18,2 cm; inner diameter: 1 cm) at ºC, under 3 MPa (ratio H 2 /HC=240) of total pressure after in situ sulfidation. The feedstock established for standard conditions contained: 4,6-DMDBT (0,66 wt.%) dissolved in cyclohexane (57,14 wt.%) and xylene (40,00 wt.%), then dimethyl disulfide (1,20 wt.%) and quinoline (1,00 wt.%) were added to generate H 2 S and NH 3, respectively. In order to evaluate the effect of H 2 S the quantity of DMDS in the liquid feedstock was increased to 2,00 wt.%. Then, to study the influence of the NH 3 partial pressure, one used the experimental results determined on previous works (feedstock containing 0,50 wt.% of quinoline) and the experimental tests done along the present work (feedstock containing 1,50 wt.% of quinoline). For all cases, the composition of the other compounds was maintained by adjusting the amount of cyclohexane. Finally, the effect of the H 2 partial pressure was studied by increasing the total operating pressure from 3 to 4 MPa. To maintain the composition of the other compounds constant the ratio H 2 /HC was increased from 240 to 320. The tests with CoMo-A, CoMo-B and CoMo-C were performed at different LHSV - 4 h -1, 3 h -1, 6,5 h -1, respectively. 2.3 Analysis The effluents were analyzed by a gas chromatography (GC). The starting oven temperature was 50 C and then increased to 67ºC at a 15ºC/min rate, prior to increasing to 290ºC at a 30ºC/min rate, in order to separate the produced organic compounds. The analytic results obtained from the GC allowed determining the conversion of the liquid feedstock. Hence, to obtain the HDS conversion of 4,6-DMDBT (%X!,!!!"!#$ ) the following equation was used: %X 4,6!DMDBT = n Products of 4,6!DMDBT conversion n 4,6!DMDBT,total 100 (Eq. 1) In addition, the conversion of 4,6-DMDBT through both HYD (%X!"# ) and DDS (%X!!" ) pathways were calculated by the following equations: %X HYD = %X DDS = n HYD n 4,6!DMDBT,total 100 (Eq. 2) n DDS n 4,6!DMDBT,total 100 (Eq. 3) In Eq. 2 and Eq. 3, n!"# and n!!" represent the number of moles of HYD products and DDS product produced during the catalytic test, respectively. 2.4 Kinetic Study In this study, the kinetic model was created in the software ReactOp Cascade, considering the decomposition of 4,6-DMDBT through three main pathways: HYD, DDS and HDA. Thus, the following reactions were inserted in the kinetic model. A!!"# B (Eq. 4) A!!!" C (Eq. 5) C!!"# B (Eq. 6) With A 4,6-DMDBT, B HYD products and C DDS product. Then, the results obtained from the experimental tests performed were inserted into the software in order to establish the kinetic model and understand how the H 2 S, NH 3 and H 2 partial pressures influence the decomposition of 4,6-DMDBT. With the kinetic model established, the reaction rate constant (k) and 2
3 the activation energy (E! ) were calculated. Finally, to determine the kinetic partial order for each component, the logarithm of the reaction rate constant was plotted as function of the logarithm of the partial pressure of H 2 S, NH 3 and H 2. 3 Results and Discussion 3.1 Impact of H 2 S partial pressure CoMo-based catalysts are known for being inhibited by H 2 S [1] [2]. In this study, the results showed the same tendency as HYD pathway has proven to be strongly inhibited (Figure 1), at high H 2 S partial pressure. The experimental tests concerning CoMo-A and CoMo-B at standard conditions (1,20% DMDS) were performed in previous works. Other explanation, which can be pointed out, is the fact that the catalysts used in this study have much more molybdenum (up to 20 wt.% MoO 3 ) than the catalysts averagely used [2] [4] [5]. Therefore, the catalysts prepared probably exhibit much more dispersed active phase due to the recent way of preparation. However, one cannot confirm this assumption because it is not possible to characterize the catalysts from the literature. So, it is possible that the catalysts prepared, in this study, contain more active sites than the catalysts stated in literature. Figure 2 DDS conversion of 4,6-DMDBT as function of temperature for the three catalysts prepared. In the graph, full lines represent the 1,2 wt.% DMDS feed and gapped lines represent the 2 wt.% DMDS. Figure 1 - HYD conversion of 4,6-DMDBT as function of temperature for the three catalysts prepared. In the graph, full lines represent the 1,2 wt.% DMDS feed and gapped lines represent the 2 wt.% DMDS. Moreover, as CoMo-C is the catalyst with the lowest activation energy, the almost negligible effect of H 2 S may confirm that, in additive impregnated-type catalysts, the adsorption of H 2 S is much weaker than on the other catalysts tested. However, the results found for the additive impregnated catalyst are difficult to discuss as it shows a low activity compared to the others. Thus, this test should be redone with a lower LHSV. Concerning the results obtained for the DDS pathway, for all catalysts the selectivity on hydrogenolysis products was enhanced (Figure 2), with higher H 2 S partial pressure which is in disagreement with literature [2] [3]. A possible explanation for why all catalysts exhibit higher DDS conversion, with higher H 2 S partial pressure, could be the existence of two distinct and specific active sites each of them being selective for one of the two reactions considered. Thus, H 2 S would adsorb favourably on the hydrogenolysis centers or closed to them and, at some point, would change the structure of these active sites. Therefore, it is possible that to reach full saturation of the catalytic surface, by H 2 S adsorption, and consequent inhibition of the S-edges, where supposedly hydrogenolysis reaction takes place [6], the H 2 S partial pressure should have to be higher. Eventually, the operating conditions presented in the literature were not the same as the conditions used in this study. In fact, regarding the feedstock composition, most part of the previous studies in this subject did not use quinoline into their model feedstock in order to evaluate the effect of H 2 S on HDS [2] [3]. Hence, one could also suggest that there is an indirect effect within the DDS pathway if H 2 S is introduced in the presence of quinoline. 3.2 Impact of NH 3 partial pressure The following results (Figure 3) show the difference between the chosen standard conditions and the condition with less concentration of quinoline. These experimental tests at lower concentration were performed in previous works as well as the tests with CoMo-A and CoMo-B at standard conditions (1,00% quinoline). As one can see in Figure 3, the HYD conversion increased for all three catalysts with a lower NH 3 partial pressure. In other words, a higher amount of quinoline increases the inhibition effect within the 3
4 hydrogenation reaction in all catalysts which is in agreement with literature [5]. In addition, it is also clear that the most impacted catalyst was the additive impregnated. work showing a stronger effect of nitrogen compounds on HYD was actually obtained with piperidine [3]. Ma et al. [7] and Turaga et al. [8] have also found from molecular modeling experiments, that the inhibition effect caused by nitrogen-based compounds could be stronger for HYD route. 3.3 Impact of H 2 partial pressure In Figure 5 are shown the performances concerning the HYD pathway from the catalytic test performed with a total working pressure of 40 bar. The experimental tests concerning CoMo-A and CoMo-B at standard conditions (30 bar) were performed in previous works. Figure 3 HYD conversion of 4,6-DMDBT as function of temperature for the three catalysts prepared. Full lines represent the 0,5 wt.% Quinoline model approximation and gapped lines represent the 1,0 wt.% Quinoline (standard conditions). In Figure 4 are presented the results concerning the DDS conversion. For CoMo-A and CoMo-B, the DDS conversion slightly decreased, for high temperatures, when using a feedstock containing a low quinoline concentration. Figure 5 HYD pathway conversion as a function of the temperature for different catalysts and total pressures, full lines represent the 30 bar and gapped lines represent the 40 bar conditions. Figure 4 DDS conversion of 4,6-DMDBT as function of temperature for the three catalysts prepared. Full lines represent the 0,5% Quinoline model approximation and gapped lines represent the 1,0% Quinoline (standard conditions). So, it seems that there was a slight inhibition of the DDS pathway. Therefore, this fact is in agreement to what was found in literature [5]. It is also noticeable that, for both dried and calcined catalysts there was a similar impact of NH 3 partial pressure. This may again point out the similar adsorption of inhibitory compounds by these two catalysts. Additionally, literature reports that DDS is more inhibited by quinoline than HYD [5]. However, at this level, this fact was not seen in the results as there was a higher apparent inhibition on the hydrogenation reaction, for all three catalysts (Figure 3). The only experimental Concerning the results obtained, one can see that the decomposition of 4,6-DMDBT through HYD route increases with the increasing of H 2 partial pressure. This fact is supported by most part of the results found in literature [3] [4] [9]. However, throughout the experimental test of the calcined catalyst (CoMo-B) there were some problems, at 300 C, associated with the data exploitation in the GC. So, one may consider that at this temperature the conversion through HYD pathway would be higher attending to the tendency of the experimental results. Thus, this test should be redone in order to better evaluate the influence of H 2 partial pressure on the calcined catalyst. In Figure 6 are shown the performances concerning the DDS pathway from the catalytic test performed with a total working pressure of 40 bar. Looking at the results, as mentioned previously, the DDS conversion for CoMo-B catalyst may not be correct taking into account that at 300 C there were some problems with the GC. Nevertheless, there is a clear decrease on the DDS conversion. The only way to explain this tendency should be to assume that 4
5 HDA pathway consecutive to DDS is enhanced. The same results were found for CoMo-A. For the additive impregnated catalyst, the decrease on DDS conversion is not as high as the one found for the other catalysts. the lowest activation energy attributed to a lower H 2 S partial pressure effect. Additionally, this may be linked to the fact that, at low H 2 S partial pressure, the catalytic surface coverage of the dried and calcined catalysts by H 2 S was already high. Thus, for a higher H 2 S partial pressure, they would be much less affected than the additive impregnated catalyst. Table 1 - Kinetic partial orders with respect to H 2S Catalyst HYD DDS HDA CoMo-A -0,9 1,1-1,1 CoMo-B -0,9 0,8-1,1 CoMo-C -1,1 0,7-1,6 Figure 6 DDS pathway conversion as a function of the temperature for different catalysts and total pressures, full lines represent the 30 bar and gapped lines represent the 40 bar conditions. In fact, for high temperatures, one can see a slight increase. However, these results might be bias considering the high LHSV used (low conversion rates). Indeed, this test should be redone, with a lower LHSV (higher contact time) in order to evaluate how the activity of additive impregnated catalyst is influenced by this working conditions than for the standard ones. 3.4 Kinetic Modelling For the three catalysts, a kinetic study was performed regarding the several tested conditions. The aim was to better understand the difference in the catalytic performances by changing the H 2 S, NH 3 and H 2 partial pressures. To evaluate the inhibition and activation effect caused by each partial pressure in each individual reaction pathway, the logarithm of the reaction constant rate determined by the modeling program was plotted as function of the logarithm of the partial pressure of H 2 S, NH 3 and H 2. Thus, the slopes obtained represent the kinetic partial orders concerning the HYD, DDS and HDA pathways. As previewed from the majority of the works published in literature, H 2 S has a negative impact on HYD pathway for all three catalysts [2] [10]. Moreover, looking particularly to the results obtained for the hydrogenation routes (HYD and HDA), one can see that the additive impregnated catalyst was the most inhibited, comparing with the other two catalysts. Surprisingly, this conflicts with the fact that the additive impregnated was the one with As can be seen in Table 2, the HYD pathway was greatly inhibited for all three catalysts by NH 3 partial pressure. Regarding the results obtained for DDS, one can notice that the kinetic orders are negative, for the three catalysts, although the experimental results show an increase on DDS selectivity for the higher NH 3 partial pressure. Actually, this probably an artefact linked to the HDA inhibition that provides higher DDS selectivity, but in appearance. Nevertheless, DDS is less inhibited than HYD. Regarding literature, this difference in the inhibition between DDS and HYD is possible, as shown by [7] and [8]. Actually, some experimental work carried out with quinoline in presence of H 2 S show that the HDN rate is highly impacted by H 2 S [11]. So the remaining quinoline could be hold responsible for the high inhibition of HYD, being known that quinoline undergoes HDN mainly by hydrogenation. Table 2 Kinetic partial orders with respect to NH 3 Catalyst HYD DDS HDA CoMo-A -1,6-0,7-2,0 CoMo-B -1,6-0,8-2,0 CoMo-C -1,5-0,4-1,9 As previewed, increasing H 2 partial pressure has a positive impact on HYD pathway for all three catalysts (Table 3). Moreover, it appears that the hydrogenation reaction for both dried and calcined catalysts is more promoted by the H 2 partial pressure than for the additive impregnated. Concerning the DDS pathway, one can point out that the changes in values found were almost negligible. 5
6 Table 3 Kinetic partial orders with respect to H 2 Catalyst HYD DDS HDA CoMo-A 1,0-0,5 1,0 CoMo-B 1,0-0,4 1,0 CoMo-C 0,7-0,3 0,4 Furthermore, the values obtained could be result of two made assumptions: - First, the acid S-H groups, present in the catalyst active sites, may be inhibited by H 2 thus leading to a lower DDS rate; - Secondly, one may also consider that these results could be due to the lack of experimental points and the error associated to the model fitting. As a consequence, at this point, one considered that DDS pathway was not modified by the H 2 partial pressure. 4 Conclusion and Perspectives In this study, the main focus was to evaluate the deep HDS of middle distillates in the range of operating conditions dedicated to the low pressure HDS with sulfided CoMo-based catalysts. Three CoMo-based catalysts were prepared and catalytic tests were performed in order to compare their performances within the same range of temperature and HDS global conversion. Moreover, the inhibiting and promoting effects of H 2 S, NH 3 and H 2 on the three catalysts were compared and discussed for each HDS pathways, namely HYD and DDS. Regarding the effect of the partial pressure of H 2 S, the three catalysts were inhibited similarly by H 2 S. Nevertheless, only the hydrogenation seems to be inhibited while DDS appears to be promoted. These results strongly disagree with the literature and could be due to the working conditions, the molybdenum amount and/or the partial pressure of nitrogen. Concerning the impact of nitrogen-based compounds (quinoline), it was found that the three catalysts undergo a strong inhibition over both pathways and especially the hydrogenation, in agreement with some literature data. Finally, concerning the effect of H 2, the catalysts showed a quite similar promoting impact although the additive impregnated was slightly less enhanced. All in all, the conditions in which the additive impregnated catalyst would relatively perform the best compared to non-additivated catalysts were with high NH 3 partial pressure, low H 2 partial pressure and relatively low H 2 S partial pressure. As perspectives for this study, an improvement regarding the kinetic model created should be done in order to fully understand the HDS of 4,6-DMDBT within the model feedstock considered. The following propositions should be taken into account: - The decomposition of quinoline should be introduced into the kinetic model to conclude if quinoline inhibits more than NH 3 or if there is some cross effect with H 2 S; - A lower amount of 4,6-DMDBT should be introduced into the model feedstock in order to study the adsorption/desorption relation between the 4,6-DMDBT and the catalytic surface. Some other perspectives, regarding the hypothesis made to explain the promoting effect over DDS with high H 2 S partial pressure, should also be considered. On one hand, the same tests should be redone for all three catalysts decreasing the amount of MoO 3 within the catalysts and/or increasing the H 2 S partial pressure, in order to directly compare the results with literature. On the other hand, the amount of H 2 S could be increased to a higher extent to observe if some inhibition occurs, providing a more accurate H 2 S partial order. Finally, all the experimental tests performed should be redone replacing the CoMo/Al 2 O 3 catalysts by NiMo/Al 2 O 3 or even without promoter (Mo/Al 2 O 3 ). This would allow understanding if the promoter used has an impact on the kinetic mechanism of the 4,6-DMDBT HDS. References [1] S. Texier et al., J. Catal., vol. 223, , [2] V. Rabariohela-Rakotovao et al., Appl. Catal. A, vol. 306, 34-44, [3] M. Egorova et al., J. Catal., vol. 241, , [4] J. Kim et al., Ener. & Fuels, vol. 19, , [5] C. Kwak et al., Appl. Catal. A, vol. 35, 59-68, [6] P. Moses et al., J. of Catal., vol. 248, , [7] X. Ma et al., Ener. & Fuels, vol. 9, 33-37, [8] U. Turaga et al., Catal. Today, vol. 86, ,
7 [9] K. Al-Dalama et al., E. & Fuels, vol. 20, , [10] X. Li et al., J. Catal., vol. 250, , [11] C. Satterfield, I. Eng. Chem. Des., vol. 20, 53,
CoMo/NiMo Catalyst Relay System for Clean Diesel Production
CoMo/NiMo Catalyst Relay System for Clean Diesel Production Yasuhito Goto and Katsuaki Ishida Petroleum Refining Research & Technology Center, Japan Energy Corporation 3-17-35 Niizo-Minami, Toda, Saitama
More informationA Practical Approach to 10 ppm Sulfur Diesel Production
A Practical Approach to ppm Sulfur Diesel Production Yuichi Tanaka, Hideshi Iki, Kazuaki Hayasaka, and Shigeto Hatanaka Central Technical Research Laboratory Nippon Oil Corporation 8, Chidoricho, Naka-ku,
More informationReactivity of several olefins in the HDS of full boiling range FCC gasoline over sulphided CoMo/Al 2 O 3
Reactivity of several olefins in the HDS of full boiling range FCC gasoline over sulphided CoMo/Al 2 O 3 Szabolcs Magyar 1, Jenő Hancsók 1 and Dénes Kalló 2 1 Department of Hydrocarbon and Coal Processing,
More informationHYDRODESULFURIZATION AND HYDRODENITROGENATION OF DIESEL DISTILLATE FROM FUSHUN SHALE OIL
Oil Shale, 2010, Vol. 27, No. 2, pp. 126 134 ISSN 0208-189X doi: 10.3176/oil.2010.2.03 2010 Estonian Academy Publishers HYDRODESULFURIZATION AND HYDRODENITROGENATION OF DIESEL DISTILLATE FROM FUSHUN SHALE
More informationMaximize Yields of High Quality Diesel
Maximize Yields of High Quality Diesel Greg Rosinski Technical Service Engineer Brian Watkins Manager Hydrotreating Pilot Plant, Technical Service Engineer Charles Olsen Director, Distillate R&D and Technical
More informationFCC pre-treatment catalysts TK-558 BRIM and TK-559 BRIM for ULS gasoline using BRIM technology
FCC pre-treatment catalysts TK-558 BRIM and TK-559 BRIM for ULS gasoline using BRIM technology Utilising new BRIM technology, Topsøe has developed a series of catalysts that allow the FCC refiner to make
More informationA Unique Way to Make Ultra Low Sulfur Diesel
Korean J. Chem. Eng., 19(4), 601-606 (2002) A Unique Way to Make Ultra Low Sulfur Diesel Whasik Min R&D Center, SK Corporation, 140-1, Wonchon-dong, Yusung-gu, Daejeon 305-712, Korea (Received 4 March
More information[Regular Paper] 1. Introduction
[Regular Paper] Methods of Activating Catalysts for Hydrodesulfurization of Light Gas Oil (Part 2) Catalytic Properties of CoMo/Al2O3 Presulfided by Polysulfides for Deep and Ultra-deep Hydrodesulfurization
More informationPrediction of Physical Properties and Cetane Number of Diesel Fuels and the Effect of Aromatic Hydrocarbons on These Entities
[Regular Paper] Prediction of Physical Properties and Cetane Number of Diesel Fuels and the Effect of Aromatic Hydrocarbons on These Entities (Received March 13, 1995) The gross heat of combustion and
More informationHydrocracking of atmospheric distillable residue of Mongolian oil
Hydrocracking of atmospheric distillable residue of Mongolian oil Ts.Tugsuu 1, Sugimoto Yoshikazu 2, B.Enkhsaruul 1, D.Monkhoobor 1 1 School of Chemistry and Chemical Engineering, NUM, PO Box-46/574, Ulaanbaatar
More informationModel test set up methodology for HDS to improve the understanding of reaction pathways in HDT catalysts. Chemical Engineering
Model test set up methodology for HDS to improve the understanding of reaction pathways in HDT catalysts David Manuel Paulo Negreiro Thesis to obtain the Master of Science Degree in Chemical Engineering
More informationReactivity of several olefins in the HDS of full boiling range FCC gasoline over PtPd/USY
Book of Abstracts European Congress of Chemical Engineering (ECCE-6) Copenhagen, 16- September 7 Reactivity of several olefins in the HDS of full boiling range FCC gasoline over PtPd/USY Szabolcs Magyar,
More informationR&D on New, Low-Temperature, Light Naphtha Isomerization Catalyst and Process
2000M1.1.2 R&D on New, Low-Temperature, Light Naphtha Isomerization Catalyst and Process (Low-temperature isomerization catalyst technology group) Takao Kimura, Masahiko Dota, Kazuhiko Hagiwara, Nobuyasu
More informationInvestigation of Isoparaffin Rich Alternative Fuel Production
Investigation of Isoparaffin Rich Alternative Fuel Production Tamás Kasza 1, Péter Solymosi 1, Zoltán Varga 1, Ilona Whál Horáth 2, Jenő Hancsók 1 1 MOL Institutional Department of Hydrocarbon and Coal
More informationRelative volume activity. Type II CoMoS Type I CoMoS. Trial-and-error era
Developments in hydrotreating catalyst How a second generation hydrotreating catalyst was developed for high pressure ultra-low sulphur diesel units and hydrocracker pretreaters MICHAEL T SCHMIDT Haldor
More informationFCC pretreatment catalysts
FCC pretreatment catalysts Improve your FCC pretreatment using BRIM technology Topsøe has developed new FCC pretreatment catalysts using improved BRIM technology. The catalysts ensure outstanding performance
More informationSTUDIES OF NITROUS OXIDE CONVERSION IN GLIDING ARC DISCHARGES
STUDIES OF NITROUS OXIDE CONVERSION IN GLIDING RC DISCHRGES K. Krawczyk a, and M. Wieczorkowski Warsaw University of Technology, Faculty of Chemistry, ul. Noakowskiego 3, -664 Warszawa, POLND bstract.
More informationClaus unit Tail gas treatment catalysts
Claus unit Tail gas treatment catalysts The TK catalyst family Figure 1: Sulphur recovery flow scheme Tail gas treatment catalysts In the refining industry today, sulphur recovery is an extremely important
More informationDEVELOPMENT AND COMMERCIALIZATION OF ATIS-2L, A HIGH ACTIVITY, LOW COST PARAFFIN ISOMERIZATION CATALYST
DEVELOPMENT AND COMMERCIALIZATION OF, A HIGH ACTIVITY, LOW COST PARAFFIN ISOMERIZATION CATALYST W.S. Graeme, M.N.T. van der Laan Akzo Nobel Catalysts ABSTRACT Akzo Nobel s high activity paraffin isomerization
More informationEffect of Pressure, Temperature and Steam to Carbon Ratio on Steam Reforming of Vegetable Oils: Simulation Study
International Conference on Nanotechnology and Chemical Engineering (ICNCS'2) December 2-22, 2 Bangkok (Thailand) Effect of Pressure, Temperature and Steam to Carbon Ratio on Steam Reforming of Vegetable
More informationResults Certified by Core Labs for Conoco Canada Ltd. Executive summary. Introduction
THE REPORT BELOW WAS GENERATED WITH FEEDSTOCK AND PRODUCT SAMPLES TAKEN BY CONOCO CANADA LTD, WHO USED CORE LABORATORIES, ONE OF THE LARGEST SERVICE PROVIDERS OF CORE AND FLUID ANALYSIS IN THE PETROLEUM
More informationUltra deep Hydrotreatment of Iraqi Vacuum Gas Oil Using Modified Catalyst
Ultra deep Hydrotreatment of Iraqi Vacuum Gas Oil Using Modified Catalyst Dr Saba A. Ghani Associate Prof. Chemical Engineering Department University of Tikrit Bentimran_ra@yahoo.com Waleed Azez Jada'a
More informationCOMPARISON OF TOTAL ENERGY CONSUMPTION NECESSARY FOR SUBCRITICAL AND SUBCRITICAL SYNTHESIS OF BIODIESEL. S. Glisic 1, 2*, D.
COMPARISON OF TOTAL ENERGY CONSUMPTION NECESSARY FOR SUBCRITICAL AND SUBCRITICAL SYNTHESIS OF BIODIESEL S. Glisic 1, 2*, D. Skala 1, 2 1 Faculty of Technology and Metallurgy, University of Belgrade, Karnegijeva
More informationDiesel hydroprocessing
WWW.TOPSOE.COM Diesel hydroprocessing Optimizing your diesel production 32 Optimizing your diesel production As an increasing number of countries move towards requirements for low and ultra-low sulfur
More informationEffect of Operating Cconditions on Hydrodesulfurization of Vacuum Gas Oil
Iraqi Journal of Chemical and Petroleum Engineering Iraqi Journal of Chemical and Petroleum Engineering Vol.9 No.2 (June 2008) 57-67 ISSN: 1997-4884 Effect of Operating Cconditions on Hydrodesulfurization
More informationApplication of In-line High Shear Mixing Process in the Oxidative- Adsorptive Desulfurization of Diesel Fuel
2014 3rd International Conference on Environment Energy and Biotechnology IPCBEE vol.70 (2014) (2014) IACSIT Press, Singapore DOI: 10.7763/IPCBEE. 2014. V70. 13 Application of In-line High Shear Mixing
More informationThe influence of thermal regime on gasoline direct injection engine performance and emissions
IOP Conference Series: Materials Science and Engineering PAPER OPEN ACCESS The influence of thermal regime on gasoline direct injection engine performance and emissions To cite this article: C I Leahu
More informationEvaluation of phase separator number in hydrodesulfurization (HDS) unit
IOP Conference Series: Materials Science and Engineering PAPER OPEN ACCESS Evaluation of phase separator number in hydrodesulfurization (HDS) unit To cite this article: A D Jayanti and A Indarto 2016 IOP
More informationStudying effects of hydrotreatment on PAC compositions in refinery streams using GC GC-FID/SCD and GC GC-ToFMS. Asger B.
Studying effects of hydrotreatment on PAC compositions in refinery streams using GC GC-FID/SCD and GC GC-ToFMS Asger B. Hansen, HTAS Presentation outline Petroleum refining Refinery streams Hydrotreatment
More informationGTC TECHNOLOGY. GT-BTX PluS Reduce Sulfur Preserve Octane Value - Produce Petrochemicals. Engineered to Innovate WHITE PAPER
GTC TECHNOLOGY GT-BTX PluS Reduce Sulfur Preserve Octane Value - WHITE PAPER Engineered to Innovate FCC Naphtha Sulfur, Octane, and Petrochemicals Introduction Sulfur reduction in fluid catalytic cracking
More informationDIESEL. Custom Catalyst Systems for Higher Yields of Diesel. Brian Watkins Manager, Hydrotreating Pilot Plant and Technical Service Engineer
DIESEL Custom Catalyst Systems for Higher Yields of Diesel Brian Watkins Manager, Hydrotreating Pilot Plant and Technical Service Engineer Charles Olsen Director, Distillate R&D and Technical Service Advanced
More informationCONTENTS 1 INTRODUCTION SUMMARY 2-1 TECHNICAL ASPECTS 2-1 ECONOMIC ASPECTS 2-2
CONTENTS GLOSSARY xxiii 1 INTRODUCTION 1-1 2 SUMMARY 2-1 TECHNICAL ASPECTS 2-1 ECONOMIC ASPECTS 2-2 3 INDUSTRY STATUS 3-1 TRENDS IN TRANSPORTATION FUEL DEMAND 3-3 TRENDS IN ENVIRONMENTAL REGULATION 3-3
More informationMethanol distribution in amine systems and its impact on plant performance Abstract: Methanol in gas treating Methanol impact on downstream units
Abstract: Presented at the AIChE Spring 2015 meeting in Austin, TX, USA Methanol distribution in amine systems and its impact on plant performance Anand Govindarajan*, Nathan A. Hatcher, and Ralph H. Weiland
More informationUnity TM Hydroprocessing Catalysts
Aravindan Kandasamy UOP Limited, Guildford, UK May 15, 2017 May 17, 2017 Unity TM Hydroprocessing Catalysts A unified approach to enhance your refinery performance 2017 Honeywell Oil & Gas Technologies
More informationPERFORMANCE OF FRESH AND REGENERATED CATALYSTS FOR RESID HYDROTREATMENT
PERFORMANCE OF FRESH AND REGENERATED CATALYSTS FOR RESID HYDROTREATMENT Isabelle GUIBARD 1, Stéphane KRESSMANN 1, Frédéric MOREL 1, Virginie HARLE 2, Pierre DUFRESNE 3 1 IFP Centre d'études et de Développement
More informationFUNDAMENTAL STUDY OF LOW-NOx COMBUSTION FLY ASH UTILIZATION SEMI-ANNUAL REPORT. Reporting Period Start Date: 05/01/1998 End Date: 10/31/1998
FUNDAMENTAL STUDY OF LOW-NOx COMBUSTION FLY ASH UTILIZATION SEMI-ANNUAL REPORT Reporting Period Start Date: 05/01/1998 End Date: 10/31/1998 Authors: Robert H. Hurt Eric M. Suuberg Report Issue Date: 10/20/1999
More informationSULFIDING SOLUTIONS. Why Sulfide?
SULFIDING SOLUTIONS Randy Alexander, Eurecat US Inc, Frederic Jardin, Eurecat SAS France, and Pierre Dufresne, Eurecat SA, consider the factors in selecting a Sulfiding method for hydrotreating units.
More informationDevelopment of improved catalysts for deep HDS of diesel fuels
Appl Petrochem Res (14) 4:49 415 DOI 1.17/s133-14-82-x ORIGINAL ARTICLE Development of improved catalysts for deep HDS of diesel fuels Syed Ahmed Ali Received: June 14 / Accepted: 29 July 14 / Published
More informationTRANSESTERIFICATION OF RAPESEED OIL BY SOLID OXIDE CATALYSTS JERRY LUIS SOLIS VALDIVIA PHD STUDENT POKE SUMMER SCHOOL SAAREMAA, ESTONIA 2014
TRANSESTERIFICATION OF RAPESEED OIL BY SOLID OXIDE CATALYSTS JERRY LUIS SOLIS VALDIVIA PHD STUDENT POKE SUMMER SCHOOL SAAREMAA, ESTONIA 2014 OUTLINE INTRODUCTION BACKGROUND EXPERIMENTAL METHOD RESULTS
More informationReport. Refining Report. heat removal, lower crude preheat temperature,
Delayed coker FCC feed hydrotreater FCCU Crude unit Hydrotreater Hydrotreater P r o c e s s i n g Better fractionation hikes yields, hydrotreater run lengths Scott Golden Process Consulting Services Houston
More informationTHE EASY TOTSUCAT SOLUTION THE WAY TO START UP YOUR HYDROTREATER
THE WAY TO START UP YOUR HYDROTREATER If you have been waiting for a catalyst that is just as easy to load as an oxidic catalyst and provides a Load & Go start-up, then TOTSUCAT EZload is YOUR activated
More informationConfirmation of paper submission
Dr. Marina Braun-Unkhoff Institute of Combustion Technology DLR - German Aerospace Centre Pfaffenwaldring 30-40 70569 Stuttgart 28. Mai 14 Confirmation of paper submission Name: Email: Co-author: 2nd co-author:
More informationResidue Upgrading in Slurry Phase over Ultra-fine NiMo/γ-Al 2 O 3 Catalyst
Scientific Research China Petroleum Processing and Petrochemical Technology 2015, Vol. 17, No. 3, pp 1-6 September 30, 2015 Residue Upgrading in Slurry Phase over Ultra-fine NiMo/γ-Al 2 O 3 Catalyst Tong
More informationThe Role of the Merox Process in the Era of Ultra Low Sulfur Transportation Fuels. 5 th EMEA Catalyst Technology Conference 3 & 4 March 2004
The Role of the Merox Process in the Era of Ultra Low Sulfur Transportation Fuels 5 th EMEA Catalyst Technology Conference 3 & 4 March 2004 Dennis Sullivan UOP LLC The specifications for transportation
More informationOnboard Plasmatron Generation of Hydrogen Rich Gas for Diesel Engine Exhaust Aftertreatment and Other Applications.
PSFC/JA-02-30 Onboard Plasmatron Generation of Hydrogen Rich Gas for Diesel Engine Exhaust Aftertreatment and Other Applications L. Bromberg 1, D.R. Cohn 1, J. Heywood 2, A. Rabinovich 1 December 11, 2002
More informationSensitivity analysis and determination of optimum temperature of furnace for commercial visbreaking unit
ISSN : 0974-7443 Sensitivity analysis and determination of optimum temperature of furnace for commercial visbreaking unit S.Reza Seif Mohaddecy*, Sepehr Sadighi Catalytic Reaction Engineering Department,
More informationDetection of Sulfur Compounds in Natural Gas According to ASTM D5504 with an Agilent Dual Plasma Sulfur Chemiluminescence Detector
Detection of Sulfur Compounds in Natural Gas According to ASTM D554 with an Agilent Dual Plasma Sulfur Chemiluminescence Detector Application Note Author Rebecca Veeneman Abstract Sulfur compounds in natural
More informationOriginal. M. Pang-Ngam 1, N. Soponpongpipat 1. Keywords: Optimum pipe diameter, Total cost, Engineering economic
Original On the Optimum Pipe Diameter of Water Pumping System by Using Engineering Economic Approach in Case of Being the Installer for Consuming Water M. Pang-Ngam 1, N. Soponpongpipat 1 Abstract The
More informationExperimental Study on 3-Way Catalysts in Automobile
, pp.44-48 http://dx.doi.org/10.14257/astl.2016.130.10 Experimental Study on 3-Way Catalysts in Automobile S. W. Lee 1, Jongmin Kim 2, Doo-Sung Baik 3 1, 2 Graduate School of Automotive Engineering, Kookmin
More informationRefComm Galveston May 2017 FCC naphtha posttreatment
RefComm Galveston May 2017 FCC naphtha posttreatment Henrik Rasmussen Haldor Topsoe Inc. Houston TX Agenda Why post-treatment of FCC naphtha? The new sulfur challenge Molecular understanding of FCC naphtha
More informationHYDROCRACKING OF FISCHER-TROPSCH PRODUCTS
HYDROCRACKING OF FISCHER-TROPSCH PRODUCTS U. M. Teles and F. A. N. Fernandes Universidade Federal do Ceará Departamento de Engenharia Química Campus do Pici, Bloco 709 60455-760 Forzaleza, CE, Brasil fabiano@efftech.eng.br
More informationCHAPTER 1 INTRODUCTION
CHAPTER 1 INTRODUCTION 1.1 Background The fossil fuel as a petroleum fuel is a limited energy resource. The dependencies on petroleum as a main energy source cannot be denied. Presently, the energy for
More informationAbstract Process Economics Program Report 246 NEAR ZERO SULFUR DIESEL FUEL (November 2002)
Abstract Process Economics Program Report 246 NEAR ZERO SULFUR DIESEL FUEL (November 2002) Desulfurization of diesel fuel is growing worldwide into a process critical to petroleum refinery profitability.
More informationRefining/Petrochemical Integration-A New Paradigm Joseph C. Gentry, Director - Global Licensing Engineered to Innovate
Refining/Petrochemical Integration-A New Paradigm Introduction The global trend in motor fuel consumption favors diesel over gasoline. There is a simultaneous increase in demand for various petrochemicals
More informationGTC TECHNOLOGY WHITE PAPER
GTC TECHNOLOGY WHITE PAPER Refining/Petrochemical Integration FCC Gasoline to Petrochemicals Refining/Petrochemical Integration - FCC Gasoline to Petrochemicals Introduction The global trend in motor fuel
More informationUOP UNITY Hydrotreating Products
Satyam Mishra UOP UNITY Hydrotreating Products 19 February 2018 Honeywell UOP ME-TECH Seminar Dubai, UAE UOP 8080A-0 2018 UOP LLC. A Honeywell Company All rights reserved. Outline 1 Unity UNITY UOP Unity
More informationEffect of Feedstock Properties on Conversion and Yields
REFINING Fluid Cata/ tic Crackin and Thermal Crackin of Vacuum Gas Oils Effect of Feedstock Properties on Conversion and Yields By D. STRA TIEV, I. SHISHKOVA, A. VELI, R. NIKOLOVA, D. D. STRA TIEV, M.
More informationA Look at Gasoline Sulfur Reduction Additives in FCC Operations
A Look at Gasoline Sulfur Reduction Additives in FCC Operations Melissa Clough Technology Specialist, BASF Refcomm Galveston 2016 Drivers for Low Sulfur Additive Worldwide legislative drive for air quality
More informationPREDICTION OF FUEL CONSUMPTION
PREDICTION OF FUEL CONSUMPTION OF AGRICULTURAL TRACTORS S. C. Kim, K. U. Kim, D. C. Kim ABSTRACT. A mathematical model was developed to predict fuel consumption of agricultural tractors using their official
More informationArticle: The Formation & Testing of Sludge in Bunker Fuels By Dr Sunil Kumar Laboratory Manager VPS Fujairah 15th January 2018
Article: The Formation & Testing of Sludge in Bunker Fuels By Dr Sunil Kumar Laboratory Manager VPS Fujairah 15th January 2018 Introduction Sludge formation in bunker fuel is the source of major operational
More informationTHERMAL AND CATALYTIC CRACKING OF PETROLEUM RESIDUE OIL
Engineering Journal of the University of Qatar, Vol. 18, 2005, pp. 1-8 THERMAL AND CATALYTIC CRACKING OF PETROLEUM RESIDUE OIL Y. Syamsuddin, B. H. Hameed, R. Zakaria, and A.R. Mohamed School of Chemical
More informationRefining/Petrochemical Integration-A New Paradigm
Refining/Petrochemical Integration-A New Paradigm Introduction The global trend in motor fuel consumption favors diesel over gasoline. There is a simultaneous increase in demand for various petrochemicals
More informationOXIDATIVE DESULFURIZATION OF MODEL DIESEL FUEL WITH HYDROGEN PEROXIDE
R. Joskić, D. Margeta, K. Setić Bionda Oxidative desulfurization... Robert Joskić, Dunja Margeta, Katica Sertić-Bionda ISSN 0350-350X GOMABN 53, 1, 11-18 Izvorni znanstveni rad / Original scientific paper
More informationJournal of KONES Powertrain and Transport, Vol. 21, No ISSN: e-issn: ICID: DOI: /
Journal of KONES Powertrain and Transport, Vol. 1, No. 1 ISSN: 131- e-issn: 3-133 ICID: 1131 DOI: 1./131.1131 JET FUELS DIVERSITY Air Force Institute of Technology Ksiecia Boleslawa Street, 1-9 Warsaw,
More informationReducing octane loss - solutions for FCC gasoline post-treatment services
Reducing octane loss - solutions for FCC gasoline post-treatment services Claus Brostrøm Nielsen clbn@topsoe.com Haldor Topsoe Agenda Why post-treatment of FCC gasoline? Molecular understanding of FCC
More informationHydrodesulfurization of sulfur-containing polyaromatic compounds in light gas oil using noble metal catalysts
Applied Catalysis A: General 289 (2005) 163 173 www.elsevier.com/locate/apcata Hydrodesulfurization of sulfur-containing polyaromatic compounds in light gas oil using noble metal catalysts Atsushi Ishihara
More informationSTUDIES ON FUSHUN SHALE OIL FURFURAL REFINING
Oil Shale, 2011, Vol. 28, No. 3, pp. 372 379 ISSN 0208-189X doi: 10.3176/oil.2011.3.02 2011 Estonian Academy Publishers STUDIES ON FUSHUN SHALE OIL FURFURAL REFINING G. X. LI, D. Y. HAN *, Z. B. CAO, M.
More informationOxidative Desulfurization of Kerosene in the Presence of Iron chloride ionic Liquid Catalyst and Ultrasound waves
ORIENTAL JOURNAL OF CHEMISTRY An International Open Free Access, Peer Reviewed Research Journal www.orientjchem.org ISSN: 0970-0 X CODEN: OJCHEG 15, Vol. 31, No. (4): Pg. 2409-2413 Oxidative Desulfurization
More informationThe influence of fuel injection pump malfunctions of a marine 4-stroke Diesel engine on composition of exhaust gases
Article citation info: LEWIŃSKA, J. The influence of fuel injection pump malfunctions of a marine 4-stroke Diesel engine on composition of exhaust gases. Combustion Engines. 2016, 167(4), 53-57. doi:10.19206/ce-2016-405
More informationInternal Combustion Engines
Emissions & Air Pollution Lecture 3 1 Outline In this lecture we will discuss emission control strategies: Fuel modifications Engine technology Exhaust gas aftertreatment We will become particularly familiar
More informationSimulation of Hydrotreating Units of Gas oil and Vacuum Gas oil
Simulation of Hydrotreating Units of Gas oil and Vacuum Gas oil Diane Dias a, *, Maria Filipa Ribeiro a, Cristina Ângelo b * diane.dias@tecnico.ulisboa.pt a Departamento de Engenharia Química, Instituto
More information1-3 Alkanes structures and Properties :
1-3 Alkanes structures and Properties : The simplest family of organic molecules is the (Alkanes). Alkanes are relatively unreactive and not often involved in chemical reactions, but they nevertheless
More informationUnderstanding Cloud Point and Hydrotreating Relationships
Understanding Cloud Point and Hydrotreating Relationships Brian Watkins Manager, Hydrotreating Pilot Plant & Technical Service Engineer Meredith Lansdown Technical Service Engineer Advanced Refining Technologies
More informationPetroleum Refining Fourth Year Dr.Aysar T. Jarullah
Catalytic Reforming Catalytic reforming is the process of transforming C 7 C 10 hydrocarbons with low octane numbers to aromatics and iso-paraffins which have high octane numbers. It is a highly endothermic
More informationBiodiesel production from waste vegetable oils over MgO/Al 2 O 3 catalyst
Biodiesel production from waste vegetable oils over MgO/Al 2 O 3 catalyst Thembi Sithole 1, a, Kalala Jalama 1,b and Reinout Meijboom 2,c 1 Department of Chemical Engineering, University of Johannesburg,
More informationAnalytical thermal model for characterizing a Li-ion battery cell
Analytical thermal model for characterizing a Li-ion battery cell Landi Daniele, Cicconi Paolo, Michele Germani Department of Mechanics, Polytechnic University of Marche Ancona (Italy) www.dipmec.univpm.it/disegno
More informationDOC design & sizing using GT-SUITE European GT Conference Gauthier QUENEY 09/10/2017
DOC design & sizing using GT-SUITE European GT Conference 2017 Gauthier QUENEY 09/10/2017 Background Simulation tool target Predict exhaust outlet emissions Thermal modeling Chemical modeling This presentation
More informationINVESTIGATION OF FRICTION COEFFICIENTS OF ADDITIVATED ENGINE LUBRICANTS IN FALEX TESTER
Bulletin of the Transilvania University of Braşov Vol. 7 (56) No. 2-2014 Series I: Engineering Sciences INVESTIGATION OF FRICTION COEFFICIENTS OF ADDITIVATED ENGINE LUBRICANTS IN FALEX TESTER L. GERGELY
More informationNEW METHODOLOGY OF DETERMINATION OF BOILING POINT AT VERY LOW PRESSURE: PETROLEUM CASE
Distillation Absorption 2010 A.B. de Haan, H. Kooijman and A. Górak (Editors) All rights reserved by authors as per DA2010 copyright notice NEW METHODOLOGY OF DETERMINATION OF BOILING POINT AT VERY LOW
More informationCatalytic Conversion of Fischer-Tropsch Waxes
CHEMICAL ENGINEERING TRANSACTIONS Volume 21, 2010 Editor J. J. Klemeš, H. L. Lam, P. S. Varbanov Copyright 2010, AIDIC Servizi S.r.l., ISBN 978-88-95608-05-1 ISSN 1974-9791 DOI: 10.3303/CET1021220 1315
More informationDefinition of White Spirits Under RAC Evaluation Based on New Identification Developed for REACH
HYDROCARBON SOLVENTS PRODUCERS ASSOCIATION Definition of White Spirits Under RAC Evaluation Based on New Identification Developed for REACH 1. Introduction Document Purpose 1.1 To facilitate substances
More informationEffect of urea/metal ratio on the performance of NiMoP/Al 2 O 3 catalyst for diesel deep HDS
Appl Petrochem Res (2015) 5:173 180 DI 10.1007/s13203-015-0098-x KACST-FRUM Effect of urea/metal ratio on the performance of NiP/Al 2 3 catalyst for diesel deep HDS Hamid Al-Megren Yu Huang Haoyi Chen
More informationScaling down/up three phase reactors
UGent Francqui Chair 2013 / 5th Lecture Scaling down/up three phase reactors Nikos Papayannakos, Professor National Technical University of Athens School of Chemical Engineering Unit of Hydrocarbons and
More informationSelected Answers to the 2010 NPRA Q&A Hydroprocessing Questions
Selected Answers to the 2010 NPRA Q&A Hydroprocessing Questions By Geri D'Angelo, Technical Service Engineer,, LLC Chicago, IL Question # 10 Brian Watkins What are refiners' experience with respect to
More informationidentify the industrial source of ethylene from the cracking of some of the fractions from the refining of petroleum Oil drilling rig
identify the industrial source of ethylene from the cracking of some of the fractions from the refining of petroleum Industrial Source of Ethylene o Ethylene is obtained industrially in 3 main steps: 1)
More informationHow. clean is your. fuel?
How clean is your fuel? Maurice Korpelshoek and Kerry Rock, CDTECH, USA, explain how to produce and improve clean fuels with the latest technologies. Since the early 1990s, refiners worldwide have made
More informationThis presentation focuses on Biodiesel, scientifically called FAME (Fatty Acid Methyl Ester); a fuel different in either perspective.
Today, we know a huge variety of so-called alternative fuels which are usually regarded as biofuels, even though this is not always true. Alternative fuels can replace fossil fuels in existing combustion
More informationExperimental investigation on constant-speed diesel engine fueled with. biofuel mixtures under the effect of fuel injection
Experimental investigation on constant-speed diesel engine fueled with biofuel mixtures under the effect of fuel injection 1 I. Vinoth kanna *, 2 K. Subramani, 3 A. Devaraj 1 2 3 Department of Mechanical
More informationTHE EFFECT OF INNER CATALYST APPLICATION ON DIESEL ENGINE PERFORMANCE
THE EFFECT OF INNER CATALYST APPLICATION ON DIESEL ENGINE PERFORMANCE Anna Janicka, Zbigniew J. Sroka, Wojciech Walkowiak Wrocław University of Technology wyb. Wyspiańskiego 27 50-370 Wroclaw tel./fax.
More informationNumerical Optimization of HC Supply for HC-DeNOx System (2) Optimization of HC Supply Control
40 Special Issue Challenges to Realizing Clean High-Performance Diesel Engines Research Report Numerical Optimization of HC Supply for HC-DeNOx System (2) Optimization of HC Supply Control Matsuei Ueda
More informationEffects Of Free Fatty Acids, Water Content And Co- Solvent On Biodiesel Production By Supercritical Methanol Reaction
Effects Of Free Fatty Acids, Water Content And Co- Solvent On Biodiesel Production By Supercritical Methanol Reaction Kok Tat Tan*, Keat Teong Lee, Abdul Rahman Mohamed School of Chemical Engineering,
More informationExperimental Investigation and Modeling of Liquid-Liquid Equilibria in Biodiesel + Glycerol + Methanol
11 2nd International Conference on Chemical Engineering and Applications IPCBEE vol. 23 (11) (11) IACSIT Press, Singapore Experimental Investigation and Modeling of Liquid-Liquid Equilibria in + + Methanol
More informationPhase Distribution of Ethanol, and Water in Ethyl Esters at K and K
Phase Distribution of Ethanol, and Water in Ethyl Esters at 298.15 K and 333.15 K Luis A. Follegatti Romero, F. R. M. Batista, M. Lanza, E.A.C. Batista, and Antonio J.A. Meirelles a ExTrAE Laboratory of
More informationFuel Related Definitions
Fuel Related Definitions ASH The solid residue left when combustible material is thoroughly burned or is oxidized by chemical means. The ash content of a fuel is the non combustible residue found in the
More informationNanofiller-modified varnishes for electrical insulation
Materials Science, Vol. 20, No. 4, 2002 Nanofiller-modified varnishes for electrical insulation B. GÓRNICKA *, J. ZAWADZKA, B. MAZUREK, L. GÓRECKI, B. CZOŁOWSKA Electrotechnical Institute Division in Wrocław,
More informationAtmospheric Chemistry and Physics. Interactive Comment. K. Kourtidis et al.
Atmos. Chem. Phys. Discuss., www.atmos-chem-phys-discuss.net/15/c4860/2015/ Author(s) 2015. This work is distributed under the Creative Commons Attribute 3.0 License. Atmospheric Chemistry and Physics
More informationHYDROGEN PRODUCTION BY AQUEOUS-PHASE REFORMING OF GLYCEROL FROM THE BIODIESEL MANUFACTURING
HYDROGEN PRODUCTION BY AQUEOUS-PHASE REFORMING OF GLYCEROL FROM THE BIODIESEL MANUFACTURING * J. Arauzo, A. Valiente, M.Oliva, J. Ruiz, L.García Thermoical Processes Group (GPT), Aragon Institute for Engineering
More informationCONSTITUTION OF COAL TAR PITCH AND ITS EFFECT ON PROPERTIES
CONSTITUTION OF COAL TAR PITCH AND ITS EFFECT ON PROPERTIES H. K. Mayer 1 and I. C. Lewis 2 1 GrafTech International Ltd., 12900 Snow Road, Parma, OH 44130 2 Consultant Introduction Corresponding author
More informationSTUDY OF CHANGES IN THE HYDROCARBON COMPOSITION OF GASOLINE AFTER EACH STAGE REFORMING REACTOR
Int. J. Chem. Sci.: 13(2), 2015, 875-884 ISSN 0972-768X www.sadgurupublications.com STUDY OF CHANGES IN THE HYDROCARBON COMPOSITION OF GASOLINE AFTER EACH STAGE REFORMING REACTOR A. E. KALDYGOZOV *, E.
More informationEXAMINATION OF THE AMMONIA DOSE INFLUENCE ON NITRIC OXIDES TRANSFORMATIONS INTO COMBINED OXIDE-PLATINUM SCR CATALYST
Journal of KONES Powertrain and Transport, Vol. 19, No. 4 2012 EXAMINATION OF THE AMMONIA DOSE INFLUENCE ON NITRIC OXIDES TRANSFORMATIONS INTO COMBINED OXIDE-PLATINUM SCR CATALYST Wojciech Kamela, Stanis
More information