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A liquid is placed in a wcll-insulatcd container, which is then scaled. Initially, the container and its contents (the liquid and pure nitrogen) are at 93°C and 1 atm; the liquid volume is 70cm3, and the gas volume is 3.00 L. The liquid partially evaporates, and the system cools down and eventually comes to thermal equilibrium at 85°C with liquid still present. Physical property data for the liquid and its vapor are:
Determine
- (See Equations 8.3-11 and 8.3-12.)
- Draw and label a flowchart for this closed system process, and write and simplify the energy balance equation, assuming adiabatic operation.
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- Problem 9.13 A 70 mm long line PQ does not have H.T. and V.T. One end of the line is 30 mm in front of the V.P. and 20 mm above the H.P. Draw its projections. Interpretation As the line PQ does not have H.T. and V.T., it is parallel to both H.P. and V.P. Construction Refer to Fig. 9.13. 1. Draw a reference line xy. Mark point p' 20 mm above xy and point p 30 mm below xy. 2. Draw a 70 mm long line p'a' parallel to xy to repre- sent the front view. X 20 p Fig. 9.13 3. Also, draw a 70 mm long line pq parallel to xy to represent the top view. 70 q yarrow_forwardProblem 10.19 A square lamina ABCD of side 40 mm is suspended from a point O such that its surface is inclined at 30° to the V.P. The point O lies on the side AB 12 mm away from A. Draw its projections. Construction Refer to Fig. 10.19. 1. First stage Draw a square a'b'c'd keeping a'd' parallel to xy. Mark a point o' on a'ď at a distance 12 mm from end a' as the point of suspension. Also, mark the centre of the square g' to represent the centre of gravity. 2. Second stage Reproduce the front view of first stage such that o'g' is perpendicular to xy. Project corners and obtain bd as the top view. 3. Third stage Reproduce the top view keeping bd inclined at 30° to xy. Obtain new points a', b', c' and ď' in the front view by joining the points of intersection of the vertical projectors drawn from points a, b, c and d of the third stage with the corresponding horizontal locus lines drawn from points a', b', c' and ď of the second stage. Join new a'b'c'd to represent the final front view.arrow_forwardProblem 10.15 A circular plane of diameter 50 mm is resting on a point of the circumference on the V.P. The plane is inclined at 30° to the V.P. and the centre is 35 mm above the H.P. Draw its projections.arrow_forward
- You are asked to manufacture 10 kg of polyester with a number-average molecular weight of 1000 by polymerizing butane-1,4-diol(HO(CH2)4OH) with adipic acid (HOOC-(CH2)4-COOH).a) What weight of diol and diacid do you need, respectively? To whatextent, p, should the reaction be carried out to? Assume a stoichiometricbalance.b) What are the number and weight fractions of dimer, trimer and tetramerat this point in the reaction?c) Because of the polymerization by dehydration to olefin, 3 mol% of thediol will be lost. What would be the number-average molecular weightwhen the reaction is carried out to the same extent? How could you offsetthis loss so that the desired molecular weightarrow_forward9.4. A PID temperature controller is at steady state with an output pressure of 9 psig. The set point and process temperature are initially the same. At time = 0, the set point is increased at the rate of 0.5°F/min. The motion of the set point is in the direction of lower temperatures. If the current settings are PART 3 LINEAR CLOSED-LOOP SYSTEMS Ke = 2 psig/°F Ti = 1.25 min TD = 0.4 min plot the output pressure versus time.arrow_forward9.6. A PI controller has the transfer function Determine the values of K, and T. 5s + 10 Ge Sarrow_forward
- 9.5. The input & to a PI controller is shown in Fig. P9-5. Plot the output of the controller if Ke 2 and 0.50 min. - E 0.5 0 -0.5 0 FIGURE P9-5 2 4 t, minarrow_forward9.3. An ideal PD controller has the transfer function P Ke (TDs + 1) E An actual PD controller had the transfer function P = Ke E TDS +1 (TDIẞ)s +1 where ẞis a large constant in an industrial controller. If a unit-step change in error is introduced into a controller having the second transfer function, show that P(1) = Kc (1 + Ae˜¯BD) where A is a function of ẞwhich you are to determine. For ẞ=5 and K = 0.5, plot P(t) versus tl tp. As ẞ, show that the unit-step response approaches that for the ideal controller.arrow_forward9.1. A pneumatic PI temperature controller has an output pressure of 10 psig when the set point and process temperature coincide. The set point is suddenly increased by 10°F (i.e., a step change in error is introduced), and the following data are obtained: Time, s psig 0- 10 0+ 8 20 7 60 90 5 3.5 Determine the actual gain (psig per degree Fahrenheit) and the integral time.arrow_forward
- 2. A unit-step change in error is introduced into a PID controller. If Ke TD = 0.5, plot the response of the controller P(t). = =10, 1, andarrow_forwardA distribution of values is normal with a mean of 211 and a standard deviation of 50.4. Find the probability that a randomly selected value is between 59.8 and 155.6. P(59.8 X 155.6) = Enter your answer as a number accurate to 4 decimal places. Answers obtained using exact z-scores or z- scores rounded to 3 decimal places are accepted.arrow_forwardTopic: Production of propylene glycol from glycerol derived from palm oil. QUESTION:Estimate capital items, operating costs and economics of the plant. Finally, report the estimatedreturn.The Detailed Factorial Method with approximately 25% accuracy must be used for detailedeconomic evaluation.Plant lifetime is fixed at 15 years.1) Depreciation and TaxesCalculate the depreciation using a suitable method (e.g., straight-line, declining balance) andincorporate tax implications based on current tax laws applicable to chemical plants. Use following attached Process Flow Diagram as reference for this question.arrow_forward
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