No full-text available
To read the full-text of this research,
you can request a copy directly from the authors.
Cost And Product Optimization of Upgrading Light Naphtha Using Pressure Swing Adsorption Method by Aspen Adsorption Simulation
Abstract
Light naphtha is an organic compound produced from the distillation process that is often sold at a low price because of its poor performance, especially in the value of Research Octane Number (RON). The goal of this study was to improve the quality of naphtha to become a useful fuel with qualifying performance that is High Optimum Mogas Component (HOMC) by using the Pressure Swing Adsorption (PSA) method with the help of Aspen Adsorption simulations to find the most optimal combination of zeolite adsorbents (Beta and 5A) to use in the process. The principle of this quality improvement is to separate the compounds contained in naphtha that have low RON values from those that have high RON values so that the performance of naphtha that has gone through the adsorption process can be maximized. For this study, the RON target from HOMC is 95, while the value of RON for feed light naphtha ranges from 61-65. There are three compounds simulated in this PSA process, n-pentane and n-hexane as compounds that want to be separated because they have low RON values from iso-pentane which has a high RON value. Furthermore, after acquiring the combination of adsorbents that resulted in the products that have the highest RON, the economic potential of all variables was evaluated to get the most optimal process to use. The economic potential is also analyzed to find the profit of the PSA process. The most optimal results are obtained when the adsorbent configuration produces the product with the highest RON and produces high economic potential. The results showed that the most optimal adsorbent combination is to use 30% Zeolite Beta; 70% Zeolite 5A with product results having the highest RON of 84 and economic potential of US$ 114,410,163.92.
... Annualized Capital Cost is the annualized value total of capital cost invested in the operation unit used, such as compressor, heater, and cooler, and operating cost invested in steam, electricity, and refrigerant. The Total Operating Cost is the cost incurred by the process operation, such as raw materials and energy costs [29]. The cryogenic distillation technology, shown in Fig. 4 However, compared to the total annual costs obtained by both technologies, CFZ technology is lower than cryogenic distillation technology. ...
The technical and economic challenges are enormous in developing gas wells with a high CO2 content (> 50 mol %), such as the East Natuna gas field, which has 71 mol % (86 mass %). Carbon capture technology in gas wells with high CO2 content is studied to find a more economical one. In this study, the technology for capturing high concentrations of CO2 is varied from gas wells, Controlled Freeze Zone (CFZ), and cryogenic distillation which will be analyzed based on cost. Variations in the CO2 content of gas wells are 75 %, 80 %, 85 %, 90 %, and 95 % in mass fraction simulated using Aspen Plus V.11.0. Based on this research, CFZ technology and cryogenic distillation can obtain purity up to 99 % and recovery above 78 %. However, the total annual cost (annual capital and operating costs) of CFZ technology is lower than cryogenic distillation technology, so CFZ technology is suitable for capturing CO2 in gas wells with high CO2 content.
... Many studies on PSA and upgrading chemical products, including naphtha, have been discussed. Anugraha et al. [8] increased the quality of naphtha to become a useful fuel with qualifying performance that is High Optimum Mogas Component (HOMC) by employing the PSA method and Aspen Adsorption simulations to determine the ideal combination of zeolite adsorbents (Beta and 5A) to utilize in the procedure. ...
The Indonesian government is optimizing the production of high-octane gasoline by utilizing existing ingredients that are plentiful and rarely used in Indonesia to keep up with the rising demand for it. Although light naphtha, a by product of the oil refinery process, has the potential to be transformed into fuel with a high Research Octane Number, its application has not yet been fully realized. The objective of this study is to carry out a study of the economic and technical feasibility of high-octane gasoline plants. A 10,000 barrel/day production potential has been built into the plant. In order to reach the RON objective of 98 for high-octane fuel, light naphtha, which has a Research Octane Number of 73, will need to be increased. The production process includes isomerization, depentanizing, and adsorption. From a technical perspective, this plant can produce high-octane gasoline from light naphtha with RON98. From an economic perspective, the Net Present Value is $ 138,247,252; Internal Rate of Return of 29.38 % per year; Pay Out Time is 3 years 5 months; and Break Even Point is 49 %. Overall, based on technical and economic perspectives, this power plant is feasible.
... Indonesia is the largest archipelagic country in the world and has the fourth largest population, with around 240 million people resulting in high energy needs. Indonesia has used fossil fuels, such as fuel oil, to meet domestic energy needs, as the primary energy source [1]. Indonesia has numerous renewable energy potentials. ...
The effects of the energy crisis and the rising energy demand have sparked development to improve efficiency in using fuel oil. According to Indonesia's oil resources, increasing refinery capacity and building mini refineries is essential to secure local refinery production. It is more effective and cost-effective to construct a small refinery with a configuration starting with a flash unit or pre-fractionator, to an atmospheric distillation unit, and a vacuum distillation unit as the last process in each oil-producing region than construct a large-scale refinery. The optimization concerned a variety of preflash furnace temperatures simulated by Aspen Plus software. The increasing temperature will change the production rate and the utility needed, which could change sales and operating costs. The result describes that the optimum profit for the mini-refinery plant is performed preflash furnace at 533 K with 108.20 US$/m3 crude oil profit.
The isomerization processes of paraffin hydrocarbons ensure a reduction in the content of aromatic and low-octane hydrocarbons in gasoline. The octane number of a commercial isomerizate largely depends on the clarity of separation of the components of the isomerization reaction mass and the degree of recirculation of non-converted paraffin hydrocarbons of normal structure. The reaction mass of the technological installation for low-temperature isomerization of the light gasoline fraction PGI-DIH, together with the target products, contains low-branched and normal hydrocarbons, in particular, up to 12% by weight of n-pentane is present in the industrial isomerizate, which degrades the quality of the commercial isomerizate due to its low octane number (RON=61.7). One of the flows of the technological scheme forming the isomerizate flow from the installation is the distillate of the deisohexanizer column, the content of n-pentane in which is up to 14.6% by weight therefore, in industrial conditions, it is advisable to extract it from the distillate of the deisohexanizer with subsequent recycling into the raw material stream. The paper proposes a change in the technological scheme of a low-temperature isomerization installation in order to maximize the extraction of raw hydrocarbons from a stable isomerizate by including a system of two additional distillation columns Cadd and DP. The research was carried out using the Honeywell Unisim Design modeling program. The calculations performed show the appropriate technological modes of operation and structural parameters of the columns: the Cadd column contains 61 three-flow valve plates, the pressure in the column Pbot = 245kPa and Ptop = 196kPa, the temperature Treb = 81.7 °С and Tcond = 47.9 °С; the DP column has 60 two-flow valve plates, the pressure Pbot = 400kPa and Ptop = 200kPa, temperature Treb = 83.4 °С and Tcond = 45.5 °С. The proposed technological scheme provides almost complete extraction of n-pentane (99.9% by weight) from a stable isomerizate with a simultaneous increase in its octane number by 2 points.
The isomerization processes of paraffin hydrocarbons ensure a reduction in the content of aromatic and low-octane hydrocarbons in gasoline. The octane number of the commercial isomerizate used in compounding in gasoline depends on the clarity of separation of the components of the isomerization reaction mass, in particular, the presence of non-converted reactants in it leads to a decrease in the octane number and loss of these raw material components. The commercial isomerization unit of a typical low-temperature isomerization unit of the light gasoline fraction PGI-DIG, together with the target products, contains low-branched and raw normal hydrocarbons, in particular, n-hexane is present, which degrades the quality of the commercial isomerization due to its low octane number (OCI= 25). One of the flows of the technological scheme forming the commercial isomerizate from the installation is the cubic product of the deisohexanizer column, the content of n-hexane in which is up to 3.5% by weight. Therefore, in industrial conditions it is advisable to extract it from the cubic product of the deisohexanizer with subsequent recycling into the raw material stream. The paper proposes a change in the technological scheme of the low-temperature isomerization installation in order to reduce the loss of raw hydrocarbons with commercial isomerization by including an additional Kdop distillation column in it. The research was carried out using the Unisim Design modeling program. The calculations performed have obtained appropriate technological modes of operation and structural parameters of the Kdop column: the number of single-flow valve plates is 30, the pressure in the Rniz column = 160kPa and Rvc = 110kPa, the temperature in the reboiler and condenser is 102.4 and 81.3 ℃, respectively, the phlegm number R = 2.5. The inclusion of an additional Kdop distillation column in a typical technological scheme ensures a reduction in losses of n-hexane with commercial isomerizate by 1.78% while simultaneously increasing its octane number by up to 2.4 points.
This study investigates the continuous adsorption treatment of gas-to-liquid (GTL) wastewater from the Fischer-Tropsch process using activated carbon fiber (ACF) as the adsorbent. ACF, characterized by a high surface area of 1232 m²/g, was utilized to treat actual GTL wastewater, which contains long and short-chain alcohols, fatty acids, and other hydrocarbons. Experimental analysis, packed-bed modeling and simulation using ASPEN Adsorption were employed to understand the dynamics of the adsorption process. The experimental setup involved a bench-scale column packed with specified masses of ACF, with GTL wastewater pumped upward through the column at varying flow rates. Breakthrough curves were constructed to assess column performance, with parameters, such as feed flow rate (5 and 10 mL/min) and packing mass (5 and 10 g) systematically varied. The results demonstrate a significant influence of these parameters on column performance, with higher flow rates initially accelerating adsorption kinetics. Conversely, increasing packing mass extends the duration of column saturation, improving efficiency. Empirical models, including the Yoon-Nelson and El-Naas et al. models were applied to fit the experimental data, with the latter showing superior performance in representing the adsorption mechanism within the column. Quantitative analysis of model fitting using Akaike Information Criteria (AIC) identified the Yoon-Nelson and El-Naas et al. model as the most suitable for describing the GTL wastewater/ACF system, with an AIC weight parameter of 0.33 and R2 averaging 86.5%. Furthermore, simulation results from ASPEN Adsorption exhibited strong agreement with experimental data, validating its efficacy for simulating liquid adsorption processes. The study provides valuable insights into the design and optimization of large-scale wastewater treatment systems, offering practical solutions to address global water challenges.
Bioethanol can be used as fuel obtained from second-generation raw material (cane bagasse) in order not to affect food sovereignty. One of the processes that have achieved a greater production and recovery of bioethanol is pressure swing adsorption (PSA), which uses zeolites to separate and purify the ethanol-water mixture. The aim of this work focuses on implementing a discrete Fault Tolerant Control and discrete PID on a virtual PSA plant for ethanol production maintaining the purity stable under the effects of combined faults in the actuator (flow valve) that can affect the PSA plant. It was observed that both controllers have great performance implementing it in the Hammerstein–Wiener model, but when performing the tests with
the PSA plant, the FTC presented greater robustness and performance (achieving a stable purity of 0.9892
molar fraction) to reduce the effects of combined faults considering changes of trajectories, on the other hand, the discrete PID presents difficulties to reduce the effect of the ramp-type fault since the purity drops to 0.82 in molar fraction. The discrete FTC achieves to produce bioethanol (above 99% wt) with purity values that international fuel standards allow.
(Proviotional share link: https://authors.elsevier.com/c/1iF2F1H~c~LlIQ)
Monoethanolamine solvent (MEA) is a common solvent used in biogas upgrading plant for carbon dioxide (CO2) and hydrogen sulfide (H2S) removal. However, it has some downsides such as corrosive, high toxicity, and promotes products degradation. Alternatively, amino acid-based solvents such as potassium lysinate (LysK) have been found to have good absorption performance. It is also claimed to be more environmentally friendly as it is less toxic and has a good biodegradability. However, its actual environmental impact for the application of biogas upgrading has not been quantified in a detailed manner. Therefore, in this study, the environmental impact of LysK solvent is quantified from gate to grave in terms of Global Warming Potential (GWP), Acidification Potential (AP) and Eutrophication Potential (EP) using life cycle assessment (LCA) approach. The process was simulated using process simulator, SuperPro Designer version 10 to obtain the input-output data. LysK solvent has a low heat of absorption, which could result in lower CO2 emissions during the biogas upgrading process. However, due to its energy-intensive nature, the incineration process significantly contributed to GWP, AP, and EP. There were also emissions of NOx and SO2 from the flue gas of the incinerator. The findings of this research provide some insight on the environmental impact of utilising LysK for biogas upgrading.
Global warming is predominantly caused by methane (CH4) and carbon dioxide (CO2) emissions. CH4 is estimated to have a global warming potential (GWP) of 28–36 over 100 years. Its impact on the greenhouse effect cannot be overstated. In this report, a dual-bed eight-step pressure swing adsorption (PSA) process was used to simulate the separation of high-purity CH4 as renewable energy from biogas (36% CO2, 64% CH4, and 100 ppm H2S) in order to meet Taiwan’s natural gas pipeline standards (>95% CH4 with H2S content < 4 ppm). Three selectivity parameters were used to compare the performance of the adsorbents. In the simulation program, the extended Langmuir–Freundlich isotherm was used for calculating the equilibrium adsorption capacity, and the linear driving force model was used to describe the gas adsorption kinetics. After the basic case simulation and design of experiments (DOE) for the laboratory-scale PSA, we obtained a top product CH4 purity of 99.28% with 91.44% recovery and 0.015 ppm H2S purity, and the mechanical energy consumption was estimated to be 0.86 GJ/ton-CH4. Lastly, a full scale PSA process simulation was conducted for the commercial applications with 500 m³/h biogas feed, and the final CH4 product with a purity of 96.1%, a recovery of 91.39%, and a H2S content of 1.14 ppm could be obtained, which can meet the standards of natural gas pipelines in Taiwan.
The aim of the present work is to monitor dew point corrosion of crude and vacuum distillation column overhead section in a petroleum refinery. The material of construction of overhead line pipe was carbon steel. The state of art of crude unit process was introduced. The corrosion and associated hydrolyzing mechanisms were briefly described. The crude processing in a petroleum refinery was extremely dynamic and thus field monitoring attempts were made, which provides some useful information on structural integrity of column downstream equipments. The demulsifier, neutralizer, and corrosion inhibitor were mixed in crude unit at specific locations for corrosion prevention. Field monitoring includes evaluation of pH and chloride content of desalter extracted water and overhead condensed water, Base Sediment & Water (BS&W) and chloride content of as‐received & desalted crude, and iron content of overhead condensed water. Furthermore, corrosion coupon was installed in overhead section to obtain the actual corrosion rate. All the field study was conducted for a specified period. The acidity, chloride concentration, and iron loss of condensed water confirmed that acidic corrosion was under control. The corrosion rate of the installed coupons confirmed that corrosion rate was within the specified limit. The results revealed in this paper intended for refinery operators and corrosion engineers involved in understanding of actual process parameters in prevention of overhead acidic corrosion.
Light naphtha is not reliable used as automotive fuel because of its low octane number (RON) and high vapor pressure. To utilize light naphtha as fuel, blending process may be used to obtain usable gasoline fuel. Diethyl carbonate (DEC) can be used as blending agent with light naphtha because its high octane number and low vapor pressure. Therefore in this work, the vapor pressure and octane number (RON) of DEC–light naphtha blends were measured to study the effect of DEC in light naphtha blending. The vapor pressure measurements show that vapor pressure of DEC–light naphtha blends decreased while the DEC fraction increased. The pseudo binary analysis approachment was used to correlate the vapor pressure experimental data and predict the vapor pressure of light naphtha + DEC blends. The Wilson and nonrandom two-liquid (NRTL) model are giving good correlation and prediction result with average absolute deviation (AAD) less than 1.3% meanwhile the Hildebrand & Scatchard model give quietly poor result with AAD value of 4.4%. The RON measurements show that the RON values of the blends increased while the DEC fraction increased. The DEC is successfully used as blending agent into light naphtha with 30% v/v optimum fraction.
This paper reports the Research (RON) and Motor (MON) Octane Numbers of gasoline blended with an oxygenated compound “ethanol”. The ethanol concentration was varied from zero to 20%, resulting in a clear picture of the variations of the RONs and MONs in all cases. The observed differences then prompt a systematic study of the variation in the RONs and MONs of ethanol blended with two type of gasoline took it in the Bazyan Oil refinery-Sulaimani and one petrol station before and after isomerization process respectively. Fuel properties of ethanol–gasoline blended fuels were first examined by the standard ASTM methods. Results showed that with increasing the ethanol content, the octane number of the blended fuels is increased until some percent after that any increase in ethanol percent will not affect RON and MON.
Corrosion monitoring is an important tool to control and predict corrosion in piping, vessels, furnace tubes, etc. of chemical plants. This study shows results from ultrasonic wall thickness measurements in crude oil and high vacuum distillation units of a German crude oil refinery. Wireless ultrasonic sen-sors were installed on the external surface of selected piping to continuously monitor internal corrosion. The focus was on high-temperature corrosion (>220°C), which is mainly caused by sulfur and acid components that are present in crude oil and its fractions. Two corrosion parameters were calcu-lated: corrosion rates (from wall thickness over time) and the change in shape of the ultrasonic back wall reflection over time (PSI). This latter parameter is derived from the ultrasonic waveform measured by each sensor. Both corrosion parameters showed different results regarding corrosion activity over time. This was explained by variations in process temperature that significantly influence wall thick-ness readings but not PSI. Furthermore, only limited correlation was found between corrosion and flow velocity/internal pressure. Finally, three crude parameters (total sulfur content, total acid number, and mercaptan content) were obtained from crude run history and compared to measuring data. Sig-nificant correlations between shape change and crude parameters were found, dependent upon sen-sor location/corrosion loop.
Abstract,— Three ,,distance—based,topological,indices,are,described; two,of them, D and D1 (mean distance topological indices, for any graphs, and for acyclic graphs, respectively) have a modest discrimi- nating,ability but may be useful for correlations, e. g. with octane numbers.,The third index, J (average distance sum connectivity) is the,least,degenerate,single,topological,index,proposed,till,now.,The properties,of this,promising,index,J are discussed,in more,detail.
Steady-state and dynamic simulation of Preflash and Atmospheric column (Pipestill) in a real crudeoil distillation plant was performed using ASPEN simulations. Steady-state simulation resultsobtained by ASPEN plus were compared to real experimental data. Experimental ASTM D86 curvesof different products were compared to those obtained by simulations. Influence of the steam flowrate in the side stripers and of the heat flow removed in pumparounds was analyzed. Significantinfluence of the heat flow removed in pumparounds on the flow conditions in the column and onthe product composition is explained.Steady-state flowsheet was completed by dynamic simulation requirements and exported to ASPENDynamics for simulations in dynamic mode. The behavior of the products flow rate in dynamicregime was observed after changing the crude oil feed by 10%. Two different control methodsbased on composition (ASTM D86 95% boiling point) and temperature at the second stage wereapplied in dynamic simulation. The time needed to reach a new steady-state, deviation, and abilityof reaching the preset parameters of both methods were compared.
As an archipelagic country, Indonesia faces challenges in supplying fuel to various regions. Some regions have small oil reserves and small fuel demand. Other regions have greater fuel demands. One solution to overcome the issue of fuel supply is to build and develop mini refineries with a scale of 6,000 – 20,000 barrels per day to maximize the potential of existing oil reserves, reach remote areas, and meet domestic demands. This study aims to analyze the feasibility of a mini oil refinery from a technical and economic perspective. The feed used for this plant is light crude oil with API gravity 47.3002 from the Belida block, South Sumatra. The plant is designed with a capacity of 10,000 barrels per day to produce intermediate products. The production process at this plant uses a simple process to reduce capital costs, which consists of a Preheater, Pre-Flash Distillation Unit, Atmospheric Distillation Unit, and Vacuum Distillation Unit. From the results of economic analysis, the obtained capital cost of IDR 517,640 million and operational cost of IDR 2,860,622 million. Meanwhile, the payback period is 4.5 years, and the break-even point is 48%. By considering the economic and technical aspects, this Mini Oil Refinery is feasible to be built.
This study utilizes zeolite 5A to separate oxygen from air in order to compare the performance of semicylindrical adsorber with that of traditional cylindrical adsorber for pressure swing adsorption by simulation. Semicylindrical adsorber can have better heat compensation during adsorption and desorption steps, which increases the oxygen purity of product in Skarstrom cycle operation. The air composition is simplified to 21% oxygen, 1% argon and 78% nitrogen. The extended Langmuir isotherm model is used to describe adsorption isotherms of gas components. The linear driving force model is used to describe the mass transfer resistance between gas and solid phase. Furthermore, the simulation program is verified with experimental data. The results show the reliability of the program and parameters. Then, we build a PSA process with semicylindrical adsorbers under appropriate operating conditions and compared it with a PSA process with traditional cylindrical adsorbers. From the results of discussing the operating variables, heat compensation of semicylindrical adsorber does increase oxygen purity for oxygen separation from air, once the adsorber changed from cylindrical one into semicylindrical one. The benefit of heat compensation is more obvious for larger adsorber, higher operating and surrounding temperature, and lower feed pressure in the range of this study.
In this work, the performance of 3A, 4A and 5A zeolites in a PSA reactor to obtain methanol by CO2 hydrogenation has been compared by numerical simulation. Henry's constants of adsorption and the reciprocal diffusion time constants of water and methanol in these adsorbents have been measured in the reaction temperature range (200-350°C) to simulate their performance using a zeolite/Cu-ZnO-Al2O3 catalyst mixture. A new cycle has been proposed for PSA reactors including a complete recirculation of heavy product, without using a purge. The best performance is obtained with 3A zeolite, having the lower water and methanol affinities facilitating bed regeneration. With the proposed process, methanol can be produced from CO2 hydrogenation at 250°C and 50 bar with a conversion of 99.6% in one step, a selectivity of 83-96%, and productivities of 0.023-0.13 mol m³ s⁻¹. The process has minimal loss of H2 in the form of water (1 mole H2O/mole converted CO2).
With an increasing focus on energy performance improvements and strict environmental laws, there is a need to recycle water resources and reuse them in the industry. Refineries consumes huge amounts of water which offer an opportunity to reprocess it in an efficient manner. This study focusses on the design and simulation of sour water stripping (SWS) unit in the refinery setup for the reuse of sour water. The stripper removes the H2S and NH3 content from the sour water making it recyclable for various processes. In this study, process simulation has been performed to analyze the energy saving and cost reducing prospects in the sour water stripping unit. Various alternative designs have been developed to seek process improvements either by improving the energy efficiency or by reducing the sour water stripping unit cost. A novel design has been proposed in this study that can reduce the energy requirement by around 53% compared to the conventional designs. The results of this study provide a meaningful analysis in terms of energy and economic considerations to improve the performance of the sour water units in the refineries.
Petroleum refineries are now facing much tighter and stricter transportation and fuel specification standards, as well as environmental regulations, than in previous years. Therefore, tough rules have been applied on gasoline specifications. Octane number is a key variable of gasoline quality. Isomerization is one of many processes that generate profit by increasing low gasoline octane numbers, with better environmental impacts compared to other processes. Here we analyzed and optimized the various variables affecting the isomerate octane numbers produced by isomerization. Feed composition (naphthenes and benzene content in the feed) and operating conditions (temperature, hydrogen consumption and liquid hourly space velocity) data were collected from the Midor isomerization plant (Egypt) over a 4-year period based on the catalyst lifetime. These data were then used to predict the influence of feed composition and operating conditions on isomerate research octane number using a Response Surface Methodology (RSM) approach (Design Expert software). Thus, we were able to predict isomerate research octane number under various operating conditions. All of the studied variables were found to influence octane number.
Dehydration is a critical operation in natural gas conditioning as it reduces the potential for corrosion, hydrate formation and freezing in process equipment and transportation pipelines. Water dew point adjustment is particularly challenging in the remote ultra-deepwater natural gas reserves of the Brazilian Pre-Salt fields due to their very high carbon dioxide contents – from 30% up to 90% in raw natural gas – which is a consequence from the carbonaceous rock of the reservoir structure and long term elevation of carbon dioxide content due to its injection for early enhanced oil recovery. Under this scenario, the study evaluates the impact of the carbon dioxide content of the natural gas on the performance of water dew point via water adsorption on 4 Å Zeolite molecular sieve beds. Process simulation with adsorption simulator Adsim (Aspen Technology, Inc), at varying operation pressures and carbon dioxide contents in raw natural gas, indicated that, although adsorption meets water removal specification in a condensation free operation, the high fugacity of carbon dioxide penalizes the dehydration performance due to probably two facts: (i) higher carbon dioxide fugacity in the humid natural gas imply higher saturation water content in the gas phase, which increases the service of dehydration units; and (ii) higher carbon dioxide fugacity in the humid natural gas establishes a discreet adsorption competition with water resulting in 6.5% increase of adsorbent bed volume for operating pressures of 35 bar or higher.
This chapter discusses the degradation issues for metallic equipment in hydrocarbon fuel conversion processes. Conversion processes cover a wide range of corrosive and fouling environments due to the different sources of fuel (crude oils, natural gas, coal, petcoke, lignin, tar sands, etc.) and a wide range of technologies (hydroconversion, cracking, oxidation, gasification, pyrolysis, etc.). The main types of degradation encountered in principal fuel conversion technologies such as high-temperature attacks by hydrogen, carbon, sulfur, chlorides, oxygen, etc., and the main types of deposits, are reviewed. The most often encountered protection and mitigation techniques will be emphasised: proper material and coating selections, and injection of additives. Best practice in plant management corrosion and scale monitoring, non-destructive techniques and inspection planning are discussed.
Generally, welding produces welding deformation and residual stress in the products, which influences the quality and performance of the products. Although many engineers and researchers have made great effort how to control these incidents, they have still remained unresolved. Welding Deformation and Residual Stress Prevention provides a unique computational approach to the prediction of the effects of deformation and residual stress on materials. The goal is to provide engineers and designers with the ability to create their own computational system for predicting and possibly avoiding the problem altogether. The basic theories including "theory of elastic-plastic analysis" and "inherent strain theory" , and analysis procedures are described using a simple three-bar model. Online simulation software to perform basic analysis on welding mechanics Examples of strategic methods and procedures are illustrated to have solved various welding-related problems encountered in the process of construction. Appendices present data bases for welding residual stresses, temperature dependent material properties, etc.
The increasing production of condensate oil due to shale gas/natural gas booming has economically motivated refiners to add this valuable and abundant crude source into their feedstock. Many refineries, however, were originally built to process heavier crudes, whose design must be retrofitted to enable the processing of the changed feedstock. The conceptual retrofit design of crude distillation units for processing condensate oil has been studied. Four retrofit designs are proposed and simulated including facilities of preflash column, atmospheric distillation unit, and vacuum distillation unit. All retrofit designs are comprehensively evaluated by steady-state modeling for feasibility check, energy consumption analysis for operating cost evaluation, and retrofit cost evaluation. The retrofit design with preflash columns in sequence potentially could be the most economical case.
The aim of this research is to get the optimum operating condition of crude distillation unit in order to get the highest profit for the crude oil refinery industry. Feed's specification data are taken from an Indonesian crude oil refinery. Simulation was done by using Aspen Plus (Aspen Technology, Inc, Burlington, MA, USA). The design variable for this research is the temperature of preflash column furnace. Optimization was done by considering the maximum profit. Based on the result in part one, where intermediate and light cold test molar flowrates and the quality of heavy naphtha in the 95% liquid volume ASTM D86 at 415 K and light kerosene distillate in the 95% liquid volume ASTM D86 at 469 K are held constant, the optimum condition is found at the furnace preflash temperature of 572 K with a profit of US 7.74 per m3 crude oil. © 2011 Curtin University of Technology and John Wiley & Sons, Ltd.
Pressure swing adsorption (PSA) is attractive for final separation in the process of water removal especially for fuel ethanol production. Despite many researches on simulation and experimental works on adsorption of water on 3A zeolite in a fixed bed, none have studied a process with the actual PSA system. The purpose of this research was to study the PSA process with two adsorbers and effects of several parameters. The research also included analysis of kinetic and thermodynamic data of ethanol-water adsorption on commercial 3A zeolites in a single fixed bed. A two-level factorial design experiment was used in this research work to preliminarily screen the influence and interaction among the factors. Effects of important parameters such as initial temperature, feed concentration and feed rate were investigated. It was proven that the Langmuir isotherm could best predict the experimental results. In the PSA pilot test, the principal factors, which had effects on the performance, were feed rate, feed concentration, adsorption pressure and the cycle time. Prediction of the process efficiency in terms of ethanol recovery and enrichment was proposed in the form of regression models. The results of the study in a fixed bed adsorber could help designing a pilot-scale PSA unit. The experiments proved to be successful in terms of producing high concentration ethanol with high percentage of ethanol recovery. With further simulation work the process could be scaled up for an industrial use.
A good approach of the critical molecular dimensions of 35 linear and branched C5–C8 paraffins by DFT quantum chemical calculations at B3LYP/6-31G** level of theory in gas phase is described. In this context, we found that either the determined molecular width or width-height average values can be used as critical measures in the analysis for selection of molecular sieves materials, depending on their pore size and shape. The molecular width values for linear and monosubstituted paraffins are 4.2 and 5.5 Å , respectively. In the case of disubstituted paraffins, the values are 5.5 Å for 2,3-, 2,4-, 2,5-and 3,4-disubstituted and for 2,2-and 3,3-disubstituted are 6.7–7.1 Å . The values for ethyl-substituted are 6.1–6.7 Å and for trisubstituted isoparaffins are 6.7. In order to select a porous material for selective separation of isoparaffins and paraffins, the zeolite diffusivity can be correlated with the critical diameter of the paraffins according to the geometry-limited diffusion concept and the effective minimum dimensions of the molecules. The calculated values of CPK molecular volume of the titled paraffins showed a good discrimination between the number of carbons and molecular size.
The oxidative coupling of methane (OCM) to ethylene is a promising alternative for the oil based industry. In this process, beside the valuable product ethylene, unwanted by-products like CO2 are produced. Hence, the gas stream has to be refined further. The process is not applied in the industry yet, because of high separation costs. This article focuses particular on the CO2 purification of the OCM product stream. Therefore a case study was done for a design task of 90% CO2 capture from 25vol% in the OCM product gas with an operation pressure of 32×105Pa. Within the article is shown, how to resolve the lack of high separation cost for the purification and the development of an integrated, energy efficient CO2 capture process for the OCM refinery is described. Therefore a state of the art chemical absorption process using monoethanolamine (MEA) was developed and optimized for the base case. Therefore Aspen Plus® with the build-in rate based model for the mass transfer with an electrolyte NRTL – approach and chemical equilibrium reactions for the water–MEA–CO2 system as well as kinetic reactions based on the MEA-REA package was applied. In order to improve the energetic process performance, gas permeation with dense membranes was studied as process alternative. For this purpose a membrane unit was developed in Aspen Custom Modeler® (ACM). The solution-diffusion model with the free-volume-theory for gas permeation including Joule–Thomson effect as well as concentration polarization (Stünkel et al., 2009) was applied successfully. Furthermore several selective materials for a composite membrane with experimentally determined parameters were studied by this model and it was found, that a matrimide membrane provides the best selectivity performance for the OCM CO2 capture. Based on this material a membrane module was installed to form a hybrid separation process in combination with the amine based absorption process. The comparison of the state of the art process with the novel hybrid separation process shows an energy saving of more than 40% for the OCM CO2 capture. In the experimental study the stand alone performance of each unit, as well as the performance of the hybrid process were studied and the results are presented in this article.
A mathematical model for PSA separation of n/iso-paraffins has been developed. A cycle described in patent literature (Minkkinen et al., US Patent 5,233,201, 1993) was simulated. Model parameters (equilibrium isotherms and kinetic parameters) were found from independent experiments in our laboratory and from correlations available on literature (axial mass and heat dispersion; film mass and heat transfer). Isothermal and adiabatic cases are studied. Simulated results were consistent with patent data. The effects of temperature, feed pressure and feed flowrate on process performance are addressed. Lower performances are obtained by decreasing temperature, feed pressure and by increasing feed flowrate.
An experimental and modeling study of the vapor-phase adsorption of C5−C6 paraffin fractions in a fixed bed of zeolite beta was addressed. Breakthrough experiments with mixtures containing n-pentane (nPEN), iso-pentane (iPEN), n-hexane (nHEX), 3-methylpentane (3MP), 2,3-dimethylbutane (23DMB), and 2,2-dimethylbutane (22DMB) demonstrate that the sorption hierarchy is temperature-dependent. At the optimum temperature of 583 K, an enriched high-octane molecule fraction of 22DMB, iPEN, and 23DMB can be selectively separated from the low-octane equimolar C5−C6 isomerate feed. For the case of feed mixtures with the typical composition of the hydroisomerization reactor product of the total isomerization process, the enriched fraction contains low research octane number (RON) nPEN, which decreases the octane quality of the product obtained. However, the use of a layered bed with zeolite 5A and zeolite beta can displace the nPEN from the enriched fraction, resulting in a maximum octane number of about 92.5 points. Aspen Adsim was used to simulate the dynamic behavior of the C5−C6 fraction in a non-isothermal and non-adiabatic bed, giving a good description of the set of experimental data. An optimal design of a mono/dibranched separation process can be achieved by properly tuning the operating temperature and the zeolite 5A/zeolite beta ratio on a layered fixed bed.
Contenido: 1) Fundamentos de vapor-fase líquida en equilibrio (VLE); 2) Análisis de las columnas de destilación; 3) Realización de una simulación en estado estacionario; 4) Optimización económica de la destilación; 5) Sistemas más complejos de destilación; 6) Cálculos en estado estacionario para la selección de la estructura de control; 7) Conversión del estado estacionario a una simulación dinámica; 8) Control de columnas más complejas; 9) Destilación reactiva; 10) Control de columnas laterales; 11) Control de fraccionadoras de petróleo.
Global energy security and Malaysian perspective: A review
- Muhammad Khattak
- Adil
Khattak, Muhammad Adil, Jun Keat Lee, Khairul Anwar Bapujee, Xin Hui Tan, Amirul Syafiq Othman, Afiq Danial Abd
Rasid, Lailatul Fitriyah Ahmad Shafii, and Suhail Kazi. "Global energy security and Malaysian perspective: A
review." Progress in Energy and Environment 6 (2018): 1-18.
Perspektif Teknologi Energi Indonesia: Tenaga Surya untuk Penyediaan Energi Charging Station
- Outlook Bppt
- Energi Indonesia
BPPT, OUTLOOK ENERGI INDONESIA 2021 Perspektif Teknologi Energi Indonesia: Tenaga Surya untuk Penyediaan
Energi Charging Station, Jakarta, 2021.
Renewable Energy of Rice Husk for Reducing Fossil Energy in Indonesia
- Hamzah Lubis
Lubis, Hamzah. "Renewable Energy of Rice Husk for Reducing Fossil Energy in Indonesia." Journal of Advanced
Research in Applied Sciences and Engineering Technology 11, no. 1 (2018): 17-22.
Getting Started: Modeling Petroleum Processes
Aspen Technology Inc. "Getting Started: Modeling Petroleum Processes." (2006).
Diesel Price Trend and Forecast
- Chemanalyst
Chemanalyst. Diesel Price Trend and Forecast.
Jet Kerosene Price Trend and Forecast
- Chemanalyst
Chemanalyst. Jet Kerosene Price Trend and Forecast.