acceleration and range for initial fuel flows were calculated. Two numerical methods‚ Euler’s integration and 4th order Runge-Kutta integration are used for calculating different parameters for the vertically launched rocket. The efficiency and the accuracy of the methods were compared. It was found out that the 4th order Runge-Kutta is more efficient than Euler’s integration method for the given time step. Also for the rocket given the optimal initial fuel mass flow rate for attaining the highest altitude
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PRODUCTION OF POTASSIUM CARBONATE FROM COCOA HUSK ASH A Process Engineering Project Report Presented to the Department of Chemical Engineering Faculty of Chemical and Materials Engineering College of Engineering Kwame Nkrumah University of Science and Technology‚ Kumasi By AMANING OSEI EMMANUEL ATTIPOE EDEM KODZO BOAKYE KWAME JUWAH CHUKWUJINDU AWELE OMENOGOR ANWULI ROSEMARY in Partial Fulfillment of the Requirements for the course Process Engineering Project April 2013. TABLE
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Chapter 4 Fundamentals of Material Balances Material Balance-Part 1 Process Classification 3 type of chemical processes: 1. Batch process – Feed is charge to the process and product is removed when the process is completed – No mass is fed or removed from the process during the operation – Used for small scale production – Operate in unsteady state March 31‚ 2009 ChE 201/shoukat@buet.ac.bd 2 Process Classification 2. Continuous process – Input and output is continuously
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Farm Court Stony Point‚ NY 10980 P: (877) 322-5800 F: (877) 322-4774 info@cedengineering.com PNEUMATIC CONVEYING SYSTEMS A pneumatic conveying system is a process by which bulk materials of almost any type are transferred or injected using a gas flow as the conveying medium from one or more sources to one or more destinations. Air is the most commonly used gas‚ but may not be selected for use with reactive materials and/or where there is a threat of dust explosions. A well designed pneumatic conveying
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monomer‚ polymer‚ and initiator. This reaction is a multistep radical reaction that includes initiation‚ propagation‚ and termination (Eq.B.1 through Eq.B.5). Figure A.1 shows a process that produces 1000 kg/hr of polystyrene in an isothermal plug flow reactor at a styrene conversion of lower than 80%. Azobisisobutyronitrile (AIBN) initiator is fed into the reactor at a concentration of 0.022 mol/L. The stream exiting the reactor is fed into an evaporator that perfectly separates unreacted styrene
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Senior Lecturer‚ Saimaa UAS Mr Tapio Tirri‚ Director‚ MUAS FiberLaboratory Mr Jari Käyhkö‚ Research Director‚ MUAS FiberLaboratory The purpose of the research was to develop new foils model for headbox screen on higher consistency level of the feed flow than foil that is used today with target feed/accept consistency being approximately 2.0%. However‚ energy consumption and pulsation level should be in same range as today’s foil type has. The study was commissioned by Andritz. The study was carried
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Equipment Design Problem set – IA 1. Crude oil‚ specific gravity of 0.887‚ flows through the piping shown in Figure. Pipe A is 50-mm Schedule 40‚ pipe B is 75 mm Schedule 40‚ and each of pipes C is 38-mm Schedule 40. An equal quantity of liquid flows through each of the pipes C. The flow through pipe A is 6.65 m3/h. Calculate (a) the mass flow rate in each pipe‚ (b) the average linear velocity in each pipe and (c) the mass velocity n each pipe. (d) What capacity and type of pump do you recommend?
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DESIGN CONSIDERATIONS * System: Ethanol – water * Feed rate: 225kmol/h * Feed composition: 28 mol% ethanol * Feed condition: 50% saturated liquid & 50% saturated vapor * 97% of ethanol recovery is required * Operating pressure: 1bar * Distillate composition: 81 mol% ethanol * Column type: Sieve tray column * Operating condition: 70% of flooding Applying material balance to the rectifying section (Eqn 01); V=L+D Applying material balance for the more volatile
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has higher measurement of flow rate compare to vegetable seeds. This result was reliable since the granular diameter of sugar was lower than vegetable seeds thus resulting a lower time consumed by coarse sugar to pass through hopper. However‚ as the orifice size was decreased‚ the flow rate was also decrease for both coarse sugar and vegetables seeds. The results of mass flow rate of experiment was quite tally with the mass of flow rate of equation. It shows decrement of flow rate as the orifice size
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Tank 7 C. Control of Surge Tank 8 i. Implementation of Controllers 8 Product Flow Fluctuation 10 Product Density Fluctuation 10 Height Fluctuation 11 ii. Effect of Tightening Limits and Reducing Tank Size 11 References 13 Appendix 13 Derivation of Transfer Functions 13 Sample Calculation 15 List of Figures Figure 1: Relative density of surge tank feed against time 1 Figure 2: Volumetric flow rate of surge tank feed against time 1 Figure 3: Xcos surge tank simulation 3
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