Optimization of Distillation Column Experiment

Optimization of distillment tug ExperimentOptimization of distillment tower in terms of energy consumption and carbon dioxide emissionSina Rad furthest1** Department of Chemical Engineering, Isfahan University of Technology, Isfahan 84156-83111, IranAbstractThe distillment is one of the energy consuming turn in worlds military ope dimensionn industry. Therefore, there must be approach for optimal single-valued function of energy and reduction of harmful gas emission much(prenominal) as carbon dioxide. The Aspen rundown Column Targeting Tool (CTT) options in a simulation environment tin can help reduce the use of energy and hence CO2 emissions. Also, the Aspen Plus degree centigrade tracking (CT) together with the Global heating Potential (GWP) options can quantify the reduction in CO2 emission. The CTT is establish on the practical near stripped-down thermodynamical condition approximation and uses thermic and hydraulic analyses of distillment pillars to identify the objects for possible column modifications. By victimisation the CO2 emission factor data descent and fuel type, the CT estimates the do CO2 emission and net carbon fee/tax on the use of a proceeds. In this study, by exploitation these Aspen plus options and in addition employ energy efficient distillation column, namely HIDiC, the way for optimization of energy consumption and CO2 emission expressed and the results compargond with effected distillation column namely RADFRAC. Finally, it was concluded that despite lower energy consumption in HIDiC, the rate of CO2 emission is twice the conventional column.Keywords Energy-efficient Distillation column, Column targeting tool, Column deluxe intricate curves, Carbon tracking, Global warming potential.Distillation is the most widely used industrial separation technology and distillation units consume a significant part of the total heating energy in the worlds process industry. The U.S. Department of Energy estimates that 40,000 distillation columns are presently in operation in the United States and consumes 4.8 quadrillion BTUs of energy 40% of the processing energy used in refining and continuous chemical processes 1 2. Although distillation is by far the most widely applied separation technology, its major drawback is the inevitable reduce of energy due to the temperature struggle betwixt the reboiler and electrical capacity which leads to a low boilers suit thermodynamic efficiency of a distillation column, e.g., below 10% 3. Therefore, improving the energy efficiency of this unit operation is important to achieving energy savings of plant. Aspen Plus Column Targeting Tool (CTT) is based on the Practical Near-Minimum Thermodynamic Condition (PNMTC) approximation representing a practical and close to reversible operation 4. It uses thermal and hydraulic analyses of distillation columns to identify the objects for possible column modifications in 1) wooden leg feed location, 2) ebbing ratio , 3) feed learn, and 4) billet condensing and/or reboiling. These modifications can reduce the utility usage and cleanse energy efficiency.The Column Targeting Tool (CTT) option can help reduce the use of energy, season the Carbon Tracking (CT) and Global Warming Potential (GWP) options can help quantify the reduction in CO2 emission in a simulation environment. Sustainability has environmental, economic, and social dimensions and requires the responsible use of re sources such as energy and reduction in CO2 emission 5. In this study, the energy and CO2 emission as the pollutant are used as the sustainability inflection in distillation column operations. This study demonstrates how to reduce and quantify the energy consumption and CO2 emissions by using the commercial software, Aspen Plus.2.1. Column targeting toolA practical near- nominal thermodynamic condition purposes a reversible column operation at minimum reflux with appropriate heat integration and hence minimal entrop y production. To achieve this, heaters and coolers with appropriate duties must be operate at each form so that the minimum reflux ratio would be result, and hence the operating line approaches the equilibrium curve. This would correspond to the distribution of reboiling and condensing loads throughout the column, and hence over the temperature range of the operation. The Aspen Plus column targeting tool for thermal outline and hydraulic analysis is helpful in identifying the objects for appropriate modifications in order to reduce utility and capital costs by improving thermodynamic driving forces, improve energy efficiency, and decrease column bottlenecking. The column-targeting tool of Aspen Plus produces the enthalpy and the exergy impairment pens based on the practical near-minimum thermodynamic condition. The enthalpy estimations larn into account the thermodynamic waiveres due to column origination and operating conditions, such as pressure drop, dual feed and side of meat products, as strong as side heat ex channelizers. The pinch point in distillation requires that there should be no side reboiling below the pinch and no side condensing above the pinch in heat-integrated columns 6.The CTT can be activated by using the related option on the Analysis / Analysis Options sheets, as buildn in portend 1.Figure 1 Analysis / Analysis Options to activate the Column Targeting Tools (CTT).Results of the column targeting analysis depend strongly on the selection of get out nominate and heavy key components in Targeting Options (Figure 2) 7.Figure 2 Analysis / Targeting Options with key component specification.Before designating light key and heavy key components for the column (refer to Table 1), the user runs the simulation and considers the column split-fractions, composition profiles, and component K-values displayed by the Plot Wizard. In case of multiple light and heavy key, if there is more(prenominal) than one light key component, the heav iest of them is selected as the light key similarly, if there is more than one heavy key component, the lightest of them is selected as the heavy key. In the default on method for this study, key components are selected based on the component K-values. The CTT has a built-in capability to select light and heavy key components for each stage of the column 4 7.Table 1 Selection of key components deep down the Targeting Options.Method Use WhenUser definedAllows you to specify the light key and heavy key components.Based on component split fractionsThis method is outmatch for sharp or near-sharp splits fractions in product streams.Based on component K-valuesThis method is best for sloppy splits.Based on column composition profilesIn principle, this method is similar to the K-value based method. It is best suited for sloppy splits and it is, in general, inferior to the K-value based method.2.2. Column constant of gravitation Composite CurveTo analyze the energy-saving potential of di stillation columns, it is common to form the temperature-enthalpy and stage-enthalpy curves, called column terrible multiform curves. Column grand mixed curves (CGCC) are based on the practical near-minimum thermodynamic condition approximation proposed by Dhole and Linnhoff 8 9, and show the theoretical minimum heating and cooling duties within the temperature range. The stage-enthalpy calculations take into account losses or inefficiencies caused by the actual column design, such as pressure drops, multiple side products, etc. Column grand composite curves display the net enthalpies for the actual and precedent operations at each stage, and the cold and hot utility requirements. Therefore, the area between the actual and the ideal operations in a column grand composite curve should be small for a thermodynamically efficient operation. Column grand composite curves are formed by solving the mass and energy balances for a reversible column operation.Simulation packages such as A spen Plus are reservation column grand composite curves readily available even for multicomponent, complex distillation column operations such as crude oil distillation. These simulators mixture the process engineer to assess the performance of an existing operation and explore the possibility of reducing utility costs by improving efficiency in energy usage. Column grand composite curves can identify targets for restructuring and modification, and may be helpful in suggesting retrofits. Some of the retrofits consist of feed conditioning (preheating or precooling), feed splitting, reflux allowance accounts, and adding side condensers and reboilers. These retrofits purpose a practical near-minimum thermodynamic loss 6.2.3. Thermal analysesThermal analysis ability is useful in identifying design objects for enhancements in energy consumption and efficiency 8 10 11. In this ability, the reboiling and condensing loads are distributed over the temperature range of operation of the c olumn. The thermal analysis of CTT produces Column Grand Composite Curves and Exergy Lost Profiles. The user makes changes to column specifications until the profiles look right based on the column targeting methodology. The CGCCs are displayed as the stage-enthalpy (S-H) or temperature-enthalpy (T-H) profiles. They represent the theoretical minimum heating and cooling requirements over the stage or temperature range of separation. This approximation takes into account the inefficiencies introduced through column design and operation, such as pressure drops, multiple side-products, and side strippers.Using the equilibrium compositions of light (L) and heavy (H) key components obtained from a converged simulation, we estimate the minimum vapor and legato flow rates leaving the homogeneous stage with the same temperatures from the following mass balances(1)(2)where and are the equilibrium mole fractions of suave and vapor streams, and the minimum amounts of the liquid and vapor streams, and the distillate. The enthalpies for the minimum vapor and liquid flows are obtained from the molar flow ratios(3)(4)where and are the molar flows of equilibrium, and the enthalpies of equilibrium vapor and liquid streams leaving the same stage, respectively. From the enthalpy balances at each stage, the net enthalpy deficits are obtained (before the feed stage)(5) (after the feed stage)(6)After adding the individual stage-enthalpy deficits to the condenser responsibility, the enthalpy values are cascaded, and plotted in column grand composite curves. This is called the top-down calculation mental process, which impart be the same as the bottom-up calculations for a stage without any feed. At the feed stage, mass and energy balances differ from a stage without feed, and finite changes of composition and temperature disturb the reversible operation. For the two procedures to yield similar results, the enthalpy deficit at the feed stage becomes(7)The values of and may be obtained from an adiabatic flash for a single phase feed, or from the constant relative volatility estimated with the converged compositions at the feed stage and feed quality. This procedure can be reformulated for multiple feeds and side products as well as different key components. A pinch point near the feed stage occurs for nearly all binary ideal mixtures. However, for nonideal multicomponent systems, the pinch point exists in rectifyingand stripping sections.A horizontal distance between the column grand composite curve pinch point and the vertical axis represents excess heat, and therefore the scope for reduction in reflux ratio. For smaller reflux ratios, the column grand composite curve will move toward the vertical axis, and hence reduce the reboiler and condenser duties, which may be estimated by(8)where is the heat of vaporization. The horizontal distance of the column grand composite curve from the temperature axis determines the targets for position a side r eboiler or side condenser at suitable temperatures (or stages). On the other hand, a sharp change in the enthalpy represents remote feed conditioning, such as poor feed quality or nonoptimal temperature. For example, a sharp change on the reboiler side may be due to a subcooled feed, and a feed preheater can be installed. Feed conditioning is usually preferred to side condensing or reboiling, since the side heat exchangers are effective at suitable temperature levels solely.Exergy () is defined the maximum amount of work that may be performed theoretically by bringing a resource into equilibrium with its surrounding through a reversible process.(9)where and are the enthalpy and entropy, respectively, and is the reference temperature, which is usually assumed as the environmental temperature of 298.15 K. A part of reachable work potential is always lost in any real process. Exergy losses represent inefficient use of available energy due to irreversibility, and should be reduced by suitable modifications 8. Exergy balance for a steady state system is(10)where is the shaft work. As the exergy loss increases, the net heat duty has to increase to enable the column to achieve a required separation. Consequently, smaller exergy loss means less waste energy. The exergy profiles are plotted as stage-exergy loss or temperature-exergy loss. In general, the exergy loss profiles can be used as a tool to examine the degradation of accessible work due to 7 8Momentum loss (pressure driving force)Thermal loss (temperature driving force)Chemical potential loss (mass slay driving force)2.4. hydraulic analysisHydraulic analysis helps identify the allowable limit for vapor fill up on the Tray place Design/ Pressure drop or Pack Rating Design/Pressure drop sheets. Tray or packing rating information for the entire column is necessary to activate the hydraulic analysis. In addition, allowable flooding factors (as fraction of total flooding) for flooding limit calculations can be specified. The default values are 85% for the vapor flooding limit and 50% for the liquid flooding limit. The liquid flooding limit specification is available only if the downcomer geometry is specified. The allowable limit for liquid flooding (due to downcomer backup) can be specified on the Tray Rating/Downcomers sheet 7. The hydraulic analysis ability helps understand how the vapor and liquid flow rates in a column compare with the minimum (corresponding to the PNMTC) and maximum (corresponding to flooding) limits. For packed and tray columns, jet flooding controls the calculation of vapor flooding limits. For tray columns, parameters such as downcomer backup control the liquid flooding limits. Hydraulic analysis produces plots for flow rates versus stage and can be used to identify and eliminate column bottlenecks 7. Graphical and tabular profiles (Figure 3 and Figure 4) help identifying targets and analysis for possible modifications by the user.The Plot Wizard (Figure 4) prod uces various plots including the typesThermal analysis The CGCC (T-H) Temperature versus EnthalpyThermal analysis The CGCC (S-H) Stage versus EnthalpyExergy loss profiles Stage versus Exergy loss or Temperature versus Exergy lossHydraulics analysis Thermodynamic Ideal Minimum Flow, Hydraulic Maximum Flow, Actual FlowFigure 3 Tabular profile for hydraulic analysis. Figure 4 Plot Wizard displays several plots as a part of Analysis and Column Targeting Tool.2.5. Heat-Integrated Distillation Column (HIDiC)As distillation is one of the most energy-intensive units in chemical process industries, many efforts have been focused on the development of distillation systems and distillation equipment in order to improve its energy efficiency. Many complex distillation configurations have been studied and proposed to improve the energy efficiency. For example, the dividing-wall distillation column or the Petlyuk column is a complex distillation scheme which has been successfully commercialized a fter several decades of research.More recently, another distillation scheme called the internally heat-integrated distillation column (HIDiC) has received extensive attention. remote the Petlyuk column, the key idea of the HIDiC leading to considerable energy savings is the combination of direct vapor recompression scheme (VRC) and the heat integration between two diabatic sections. The diabatic section is a column section which allows heat dispatch to enter or leave its stages. Its purpose is to distribute exergy loss from the main condenser or reboiler to all stages in the section, hence reducing the main utility load and the overall exergy loss of the section. If two diabatic sections with opposite directions of heat transfer are integrated, the energy requirement along twain sections can then be saved. As shown in Figure 5a, the rectifying and the stripping sections are separated by the feed tray. Instead of having heat rejection only through the main condenser and heat suppl y through the main reboiler, the total heat rejection is distributed along the rectifying section, while the stripping section absorbs this amount of heat with similar distribution along the column. A compressor and a throttling valve are used to manipulate the pressure difference between both column sections. The rectifying pressure must be sufficiently high to provide a positive temperature driving force between both sections for feasible heat transfer along the columns. This internal heat integration between column sections can be achieved using a heat transfer equipment such as heat pipes at any stage location. The design without any thermal utility (as in Figure 5a) is called the ideal HIDiC. This scheme requires only electricity or mechanical power for compressor. However, a trim-condenser and/or trim-reboiler may be installed at the top of the rectifying and/or the bottom of the stripping sections, respectively, to enhance the process operational flexibility. The general HIDi C scheme with any trim-condenser and/or trim-reboiler is known as the internally heat-integrated distillation column (Figure 5b) 12.Figure 5 The ideal HIDiC (a) and the internally heat-integrated distillation column (b).2.6. Sustainability prosody2.6.1. Potential environmental impactThis study quantifies the sustainability metrics of potential environmental impacts, which is the emissions per unit mass of product and carbon tax, by using the Aspen Plus options of (1) Carbon Tracking (CT) and (2) Global Warming Potential (GWP).Carbon tracking In each utility block, carbon tracking allows the calculation of CO2 emissions after specifying CO2 emission factor data source and ultimate fuel source from built-in data. The CO2 emission factor data source can be from European Commission decision of 2007/589/EC or United States Environmental Protection Agency Rule of E9-5711 13 14. This source can also be directly specified by the user. In this example, CO2 emission factor data source is US-E PA-Rule-E9-5711 and the fuel source is natural gas as seen in (Figure 6). The utilities used in the column include cooling water and steam. The Results Summary / Operating Costs / Utility Cost Summary sheet displays the total heating and cooling duties as well as their costs. The rate and cost of CO2 emission results would be available within the Results Summary / CO2 Emissions.Figure 6 Utilities / U-2 / Input / Carbon Tracking / Calculate CO2 emissions.Global warming potential Aspen Plus reports greenhouse gas emissions in terms of CO2 equivalents of Global Warming Potential (GWP). CO2 is one of the greenhouse gases that cause around 20% of GWP. To use this feature one can create a property set. Prop-Set properties report the carbon equivalents of streams based on data from three popular standards for reporting such emissions 1) the IPCCs 2nd (SAR), 2) 4th (AR4) Assessment Reports, and 3) the U.S. EPAs (CO2E-US) proposed rules from 2009 (Table 2) 13 14. Prop-Set properties are acc ount in stream reports after selected Report Options / Streams / Property sets. The Setup / Calculation Options / Calculations sheet activates the standards for Global Warming Potential as well as Carbon fee/tax which set as USEPA (2009) and 5 $/lb, respectively. The Results sheet of each Utility block displays the CO2 equivalents emitted by this utility in each unit operation block where it is used.Table 2 Standards for reporting CO2 emissions.Standards for reporting CO2 emissions Prop-Set properties corresponding to each standardIPCC SAR (1995)CO2E-SARIPCC AR4 (2007)CO2E-AR4USEPA (2009)CO2E-US2.6.2. Energy intensityThis study calculates the sustainability metrics Energy intensity as nonrenewable energy per unit mass of products by using the Aspen plus Column Targeting Tool abilities of Thermal Analysis and Hydraulic Analysis.2.7. Methods for optimization2.7.1. Modifying the feed stage locationIn Aspen Plus, the condenser is the first stage, while the reboiler is the last stage. Th e S-H plots of CGCC can identify distortions because of inappropriate feed placements. The distortions become unornamented as significant projections at the feed location called the pinch point due to a need for extra local reflux to compensate for inappropriate feed placement. A correctly introduced feed removes the distortions and reduces the condenser and reboiler duties.If a feed is introduced too high up in the column, a sharp enthalpy change occurs on the condenser side on the S-H CGCC plot the feed stage should be moved down the column.If a feed is introduced too low in the column, a sharp enthalpy change occurs on the reboiler side on the S-H CGCC the feed stage should be moved up the column 10.2.7.2. Modifying the reflux ratioThe horizontal gap between the T-H CGGC pinch point and the ordinate represents the excess heat, and therefore, the scope for a reduction in reflux ratio 7. As the reflux ratio is reduced, the CGCC will move towards the ordinate and hence reduce both the reboiler and condenser duties. However, to preserve the separation, the number of stages must increase.2.7.3. Feed conditioningThe need for an adjustment of feed quality can be identified from sharp enthalpy changes on the S-H or T-H CGCC plots.If a feed is excessively sub-cooled, the T-H CGCC plot will show a sharp enthalpy changes on the reboiler side, and extent of this change determines the approximate feed heating duty required.If a feed is excessively over-heated, the T-H CGCC plot will show a sharp enthalpy changes on the condenser side, and extent of this change determines the approximate feed cooling duty required.Changes in the heat duty of pre-heaters or pre-coolers will lead to similar duty changes in the column reboiler or condenser loads, respectively.2.7.4. Side condensing or side reboilingFeed conditioning is usually preferred to side condensing or side reboiling. Side condensing or side reboiling is external modification at a accessible temperature level. The s cope for side condensing or side reboiling can be identified from the area below and/or above the CGCC pinch point (area between the ideal and actual enthalpy profiles). This area could be reduced by integrating side condensing and/or reboiling on an appropriate stage 15. If a significant area exists above the pinch, a side reboiler can be placed at a convenient temperature level. This allows heat supply to the column using a low-cost hot utility, hence minacious the overall operating costs. If a significant area exists below the pinch, a side condenser can be placed at a convenient temperature level. This allows heat removal from the column more effectively and by a cheaper cold utility, hence lowering the overall operating costs.Use of side condensing or reboiling cause increasing of a condenser and reboiler duties, an increase of CO2 emission, and an increase of costs (due to installing heat exchanger). Therefore, should be careful of using this.By using maintained above methods , CGCC plots achieved. Referring to these plots, optimal condition is where ideal and actual plots are overlapping (for S-H and V-S plots) or minimum exergy loss is obtaining (for S-E plot). Therefore, modifying conditions (such as feed stage location, reflux ratio, feed conditioning, and side condensing/reboiling duty) continued until overlapping or minimizing achieved. In the following, schematic of simulations and enter data along with their results are coming.Figure 7 Simulation of HIDiC configuration.