2. Table of Content Introduction of heat exchanger. Design of Coolers. Introduction of fixed bed reactors. Design of reactors.

3. Heat exchanger Heat exchanger is a device designed to transfer heat from one fluid (liquid or gases) to another where the two fluids are physically separated. In our design we assumed that the cooler which used is a shell and tube heat exchanger. The advantages of shell and tube heat exchanger are: 1.The configuration gives a large surface area in a small volume. 2.Can be constructed from a wide range of materials. 3.Easily cleaned.

4. Main design procedure: 1.Heat load,(kW) 2. Log mean Temperature, (˚C) Where - Inlet shell side fluid temperature ( ˚ C). - Outlet shell side fluid temperature ( ˚ C). - Inlet tube side temperature ( ˚ C). - Outlet tube temperature ( ˚ C).

5. 3.Provisional Area, (m 2 ) Where - True temperature difference. - ( Temperature correction factor) 4. Area of one tube, m 2. Where -Outer diameter (d o ), (mm) -Length of tube (L), (mm) - Number of tubes = provisional area / area of one tube  t F

6. 5. Overall heat transfer coefficient, W/m 2 o C. Where - Outside coefficient (fouling factor). - Inside coefficient (fouling factor). 6. Bundle diameter. Where - Outside diameter (mm). - Number of tubes. -K1 & n1 are constant.

7. 7. Shell diameter. 8. Shell thickness. Where - t: shell thickness (in). - P: internal pressure (psig). - r i : internal radius of shell (in). - E J : efficiency of joints. - S: working stress (psi). - C c : allowance for corrosion (in).

8. Results CoolerEquipment name To cooled the feed stream and prepare it to inter the absorber Objective E-100Equipment Number Shell and tube heat exchanger Type After the compressor K-101 Location Chilled waterUtility Carbon steelMaterial of construction Quartz wool – Glass wool Insulation 659.42Shell Side Inlet temperature (oC) 30 Shell Side Outlet temperature (oC) 15 Tube Side Inlet temperature (oC) 199.26Tube Side Outlet temperature (oC)

9. 8048.24Heat load (kW) 300Overall heat transfer coefficient (W/m 2 o C) 137.518LMTD ( o C) 518Number of tubes 2.66Tube length (m) 1.653 Tube diameter (m) 216.76Heat Exchanger area (m 2 ) 60.3Thickness (mm) 1.74Shell diameter (m) 4Number of tube Rows 107,000Cost $

10. CoolerEquipment name To cooled the solvent for recycle Objective E-104Equipment Number Shell and tube heat exchanger Type Before pump P-100 Location sea waterUtility Carbon steelMaterial of construction Quartz wool – Glass wool Insulation 64.465 Shell Side Inlet temperature (oC) 33 Shell Side Outlet temperature (oC) 25Tube Side Inlet temperature (oC) 53Tube Side Outlet temperature (oC)

11. 23411.467Heat load (kW) 300Overall heat transfer coefficient (W/m 2 o C) 9.64 LMTD ( o C) 8012 Number of tubes 7.14Tube length (m) 5.479 Tube diameter (m) 8991.6778 Heat Exchanger area (m 2 ) 10.2Thickness (mm) 5.569Shell diameter (m) 4Number of tube Rows 258,900Cost $

12. Improvement I tried to decrease the load of the cooler by using multi-stage compressors.

13. Reactors In our plant, the reactor used is catalytic fixed bed reactor. It is used very commonly in industry because it has many valuable features such as: 1.It gives the highest conversion. 2.Efficient heat transfer. 3.Temperature uniformity. 4.Less severe pressure drop.

14. Design Procedure of Catalytic Fixed Bed Reactor 1.Calculate the concentration of propane from yield. 2.Get reaction rate constant (k). 3.Calculate the partial pressure for propane and carbon dioxide.

15. 4. Calculate the rate of reaction. 5. Calculate the weight of catalyst. 6. Calculate the volume of reactor. 7. Assume the diameter of reactor. 8. Calculate the height of reactor. 9. Calculate the thickness of reactor. 10. Calculate the cost.

16. Results reactorEquipment name To convert CO2 and propane to propylene Objective CRV-100Equipment Number Catalytic fixed bed reactorType After heater E-100Location Carbon steelMaterial of construction Quartz wool – Glass wool Insulation 550Operating temperature (oC) 14.696Operating pressure (psia) 553.38 Feed Flow Rate (mole/s) 45Conversion

17. 2914.963 Weight of Catalyst (Kg) 2Number of beds 3.36Height of Bed/s (m) 2.166Volume of reactor (m 3 ) Cr2O3/SiO2Catalyst Type 1570Catalyst Density (Kg/m3) 5.7 Reactor Height (m) 0.84Reactor Diameter (m) 10Reactor thickness (m) 5,100Cost $

18. 27373.07 Weight of Catalyst (Kg) 2Number of beds 7.082Height of Bed/s (m) 20.34Volume of reactor (m 3 ) Cr2O3/SiO2Catalyst Type 1570Catalyst Density (Kg/m3) 10.35 Reactor Height (m) 1.77Reactor Diameter (m) 10Reactor thickness (m) 26,100Cost $

19. reactorEquipment name To convert CO2 and propane to propylene Objective CRV-101Equipment Number Catalytic fixed bed reactorType After heater E-101Location Carbon steelMaterial of construction Quartz wool – Glass wool Insulation 550Operating temperature (oC) 14.696Operating pressure (psia) 683.2 Feed Flow Rate (mole/s) 45Conversion

20. reactorEquipment name To convert CO2 and propane to propylene Objective CRV-102Equipment Number Catalytic fixed bed reactorType After heater E-102Location Carbon steelMaterial of construction Quartz wool – Glass wool Insulation 550Operating temperature (oC) 14.696Operating pressure (psia) 754.7 Feed Flow Rate (mole/s) 45Conversion

21. 128085.598 Weight of Catalyst (Kg) 2Number of beds 11.85Height of Bed/s (m) 95.18Volume of reactor (m 3 ) Cr2O3/SiO2Catalyst Type 1570Catalyst Density (Kg/m3) 16.31 Reactor Height (m) 2.96Reactor Diameter (m) 10Reactor thickness (m) 80,600Cost $

22. reactorEquipment name To convert CO2 and propane to propylene Objective CRV-103Equipment Number Catalytic fixed bed reactorType After heater E-103Location Carbon steelMaterial of construction Quartz wool – Glass wool Insulation 550Operating temperature (oC) 14.696Operating pressure (psia) 793.9 Feed Flow Rate (mole/s) 30Conversion

23. 183715.9Weight of Catalyst (Kg) 2Number of beds 13.358 Height of Bed/s (m) 19.503Volume of reactor (m 3 ) Cr2O3/SiO2Catalyst Type 1570Catalyst Density (Kg/m3) 18.19 Reactor Height (m) 3.34Reactor Diameter (m) 10Reactor thickness (m) 104,900Cost $

24. Improvement -In the fourth reactor we get the highest cost because it is very large in volume, so I tried to decrease the cost by changing the conversion of the propane to the value of 30%, that’s will be better for the cost and it doesn't effect highly of the production of propylene.

25. Cost of reactor Conversion of propane $1,024,3000.45 $317,0000.4 $170,4000.35 $104,9000.3 $68,2000.25 $45,1000.2 $29,3000.15 $17,9000.1

26. Thank you for listening