Make sure that your name is in the document title before uploading it to the correct assignment (i.e.Find the Exercise 4 assignment in the Lesson 5 Module by either clicking Next until you find it or by clicking Assignments and scrolling down until you find it.
#HOW TO READ DEPRIESTER CHART PDF#
Once you have a solution to the exercises you will submit your answers as a PDF by uploading your file to be graded. The rest should be type-written for ease of reading when grading. 3) read value off of the specimens curve where it intersects with the line you drew. Access to the complete content on Oxford Reference requires a subscription or purchase. How do you find values from a DePriester chart 1) make 2 points. The scanned pages should relate to using the graphs for solving the problem. Nomographs that present the complex relationships between pressure, temperature, and K-factor for various light and heavy hydrocarbons.
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Depriester chart pdf.DePriester Charts provide an efficient method to find the vapor-liquid equilibrium ratios for different substances at different conditions of pressure and temperature. Use sliders to change the pressure and temperature a. Select one of three hydrocarbons: methane, propane, or n-decane.
#HOW TO READ DEPRIESTER CHART SERIES#
Important Note: You may submit scanned images or clear handwritten pages as a PDF that is less than 2 MB in size for this exercise. K (or DePriester) Chart (low T range) in American Engineering Units from Introduction to Chemical Engineering Thermodynamics (7th ed) by Smith, J.M., Van Ness, H.C., and Abbott, M.M. This simulation applies a DePriester chart, a set of nomograms, to find the vapor-liquid equilibrium ratio (the gas phase mole fraction divided by the liquid phase mole fraction, known as the K-value) for a series of hydrocarbons. Submit your answers as a PDF in the Exercise 4 assignment inside the Lesson 5 Module, showing all the steps in your calculations, indicate the K values you read from the nomograms, and state your assumptions, if any. Would the summer, or winter asphalt product be “heavier”? Explain why. Using the DePriester Chart for Vapor Liquid Equilibrium (simulation) mirror. Explain which of the following switches will take place in the refinery in about a month, and why? 40 ptsĪ) Switch the deasphalting solvent from propane to pentane.ī) Switch the deasphalting solvent from pentane to propane. In late fall this refinery switches operations to produce more fuel oil from VDR for the coming winter months, producing still some asphalt, but in lower quantity. Vapor pressures Pt are known since temperature is given.A refinery in Northwest Pennsylvania produces asphalt as an important product that brings revenue, particularly during the summer months. Total system pressure is easily calculated (with no iteration involved) from: In this case temperature T and liquidphase composition are known. The check boxes below the sliders allow switching on and off labels and legends in the diagram. The liquid moving down the column gets richer and richer in heavy components.īubble-Point Pressure Calculation. With the right key pressed down the chart can be moved. The vapor rising in the column gets richer and richer in light components at each stage. This illustrates precisely why a distillation column can be used to separate chemical components. O-Xylene, on the other hand, the heaviest component, has a higher concentration in the liquid than in the vapor. Benzene, the lightest component, has a higher concentration in the vapor than in the liquid. New comments cannot be posted and votes cannot be cast. The numbers are almost impossible to read on my charts. Notice the enriching of lighter component that occurs in the vapor in the above example. Does anyone have access to a large DePriester chart that is legible I can only find small or pixelated versions.
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When convergence has been achieved, calculate vapor compositions. If Pctc is greater than PT, decrease T.Ħ. Check to see if Pctc is sufficientiy close to PT.ĥ. Calculate vapor pressures of all components at T.Ĥ. The calculation procedure is iterative:Ģ. This is by far the most common type of calculation encountered in distillation work because column pressure is usually known. The problem is to calculate the unknown temperature or pressure and the composition of the vapor phase (j>y).īubble-Point Temperature Calculation. In addition we must be given either the pressure or the temperature of the system. In all bubble-point calculations, we know the composition of the liquid (x/s are all given).