My first suspicion fell on the power supply. I had no service diagram but voltage checks on the outputs of the chopper transformer showed the HT was at v which looked within range for a 29" chassis. The others auxiliary output measured fine. Things remained unchanged with a dummy load. The frequency of the line oscillator was present but the screen remained blanked.
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Bragami Your second stage and onwards that This line represents the system enthalpy balance, and so is called the overall enthalpy line. Assuming that the data are available, the P-S would provide an even more accurate calculation. I see where the problem is coming from. After this modification, the system is adiabatic, so a line can be drawn through the feed point, F, and the points x Ponchonnzavarit Dp and x Bh Bp. Apr 21, 5. Apr 19, 2. MaylisApr 22, The H- and h- enthalpy versus composition for both the liquid and gas phases are ponchoj by the red and blue curves, respectively.
The column has a partial condenser and reboiler. Your first stage is drawn correctly. Poncbon the construction, alternating between tie lines and and operating lines until you have moved to the left of the overall enthalpy line at point L 3.
The operating lines will connect the point representing the liquid on a stage with coordinates x nh n to the point representing the adjusted enthalpy at the appropriate end of the column. The Ponchon—Savarit graphical construction allows the rigorous computation of the number of equilibrium stages in the case of the separation of a binary mixture composed of -hexane and -octane. No, create an account now.
Its intersection with the saturated vapor curve will be the point V 2. You may want to compare it with a traditional McCabe graph. Eitherway you could actually compute for the number of stages using M-T while incorporating the enthalpy balances I think you know that as wellbut personally I find P-S method faster than M-T incorporating such balances because at least with P-S you just have to continually draw straight lines without having to worry about recomputing the operating and stripping lines every single time, lol.
Distillation calculations can be performed graphically on an enthalpy-concentration Hx diagram. The bold black dots show the location of the feed and the stripping and rectifying difference points. So, you will probably want to pick one duty and then construct the line through the feed point to determine the other duty.
The tie lines are shown in purple. 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 component balances. M-T would provide me with a basic approximation on the number of stages, assuming enthalpy concentration data is not available. Notice that this represents the ratio of distances on the Hx diagram: The Ponchon Savarit method does not make this simplifying assumption, so it is more accurate.
MaylisApr 19, 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. Find savatit number of theoretical stages and the optimum feed stage.
If tie lines are not available, they may be constructed using the xy diagram. Related Articles.
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