This approach is sometimes called the Ponchon-Savarit Method. Working on the Hx diagram is more general than a McCabe-Thiele construction, because it. Modified versions of the Ponchon-Savarit and McCabe-Thiele methods are presented which incorporate a correct analysis of the feed region in the case of partly. 18 Nov In this work, a theoretical stage-to-stage study of a HIDiC based on the Ponchon− Savarit method is performed. Several HIDiC design variables.
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Ponchon-Savarit Graphical Equilibrium Stage Method – Wolfram Demonstrations Project
The “pinch point” also expands, ponchon savarit method in a single line where the operating and tie lines overlap. This can be used to determine the minimum number of stages. Related Topics Ponchon savarit method Engineering Chemistry. These in turn are used with the reflux ratio to get h Dp. The column has a partial condenser and reboiler.
Ponchon-Savarit Graphical Equilibrium Stage Method
So, you will probably want to pick one duty and then construct the line through the feed point to determine the other duty. The Ponchon—Savarit graphical construction allows the rigorous computation of the number of equilibrium stages in the case of ponchon savarit method separation of a binary mixture composed of -hexane and -octane.
The equilibrium data is represented by the equilibrium tie lines on the Hx diagram. Construction continues until L 5 which is almost directly on top of ponchon savarit method B.
The column is to operate at 1 atm. A similar procedure can swvarit followed on metod Hx diagram, except instead of using component balances, enthalpy balances are used.
If tie lines are not available, they may be constructed ponchon savarit method the ponchon savarit method diagram. Thus, it is useful to redefine our distillation system to be adiabatic, by bringing ponchon savarit method condenser and reboiler inside the system boundary. A feed containing 40 mole percent n- hexane and 60 percent n- octane is fed ponchon savarit method davarit distillation column. The D’ point on the Hx diagram can then be placed at 0. A calculation often begins by using the overhead product composition and temperature to obtain h D and H y1.
The operating lines will connect the point representing the liquid on mdthod stage with coordinates x nh n to the point representing the adjusted enthalpy at the appropriate end of the column. The overhead product is 95 percent hexane and the bottoms 10 percent hexane. Equilibrium data is collected. You can set values for the feed quality and feed, distillate, and bottom compositions to obtain the corresponding Ponchon—Savarit graphical construction and the number of column stages.
This line represents the system enthalpy balance, and so is called the overall enthalpy line. After this modification, the system is adiabatic, so a line can be drawn through the feed point, F, and the points x Dh Dp and x Bh Ponchon savarit method.
Rearranging the enthalpy balance gives: Distillation calculations can be performed graphically on an enthalpy-concentration Hx diagram. The operating lines are developed from enthalpy balances on the rectifying and stripping sections just as in the McCabe-Thiele approach operating equations were developed from the equivalent ponchon savarit method balances.
The reflux is a saturated liquid and feed enters the column at the optimum stage. The tie lines ponchon savarit method shown in purple.
These values and the reflux ratio can be used to find the enthalpy coordinate for the D’ point, H Dp.
RMP Lecture Notes
Points for the feed and product can be located on the Hx diagram; for our purposes we’ll call them the F, D, and B points. While doing constructions on the yx diagram, a “pinch” was defined as the intersection point ponchon savarit method the equilibrium curve and the operating curve.
Follow the tie line that passes through the V 1 point back to the saturated liquid curve. This graphical method uses both material and energy balances to determine ponchon savarit method number of theoretical stages required to achieve a specific separation.
Assume that a total condenser is used. These were ponchon savarit method paired with savsrit equilibrium curve, which relates the composition of liquid on a stage to the vapor leaving the stage. The intersection is the point L 1 liquid on tray 1.
The value of is determined by the program and the ratio of reflux to distillate flow rates at the top stage is chosen such ponchon savarit method. Its intersection with the saturated vapor curve will be the point V 2.
ponchon savarit method Plot the feed and product points. On an Hx diagram, there isn’t an equilibrium curve — it has expanded to a region, and each ponchon savarit method from the xy equilibrium curve is represented by a tie line.
This approach is sometimes called the Ponchon-Savarit Method. If the products are saturated liquid, as is the case for total condensers without subcooling and for partial reboilers, these points will lie on the bubble point curve on the Hx diagram.
The operating lines for the stripping and rectifying sections are shown in cyan and green, respectively. If the saturation curves show significant changes in curvature or separation, it suggests that to assume equimolar ponchon savarit method will introduce error.
If the dew point and bubble point lines are more or less straight and roughly parallel, it indicates that the latent heat of vaporization is basically constant with respect to composition. Al-Baghli, and Brian G. A ponchon savarit method ratio of 1. At total reflux, operating lines are vertical infinite slope. The steady-state enthalpy balance for a distillation column is: Not that operating curves are not required to do this — only ponchon savarit method endpoint compositions.
Construct an operating line through both the L 1 point and the D’ point. Some equations in this document are being displayed using MINSEa browser independent approach to displaying equations on the web. The coordinates are their composition and enthalpy.