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Separation of Boron from seawater Chemical and Petroleum Engineering Department

Training and Graduation Project Unit Graduation Project II . Separation of Boron from seawater Chemical and Petroleum Engineering Department. Department Advisor : Dr. Monwar Hussein Examiner committee: Dr. Ali Al- Naqbi

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Separation of Boron from seawater Chemical and Petroleum Engineering Department

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  1. Training and Graduation Project UnitGraduation Project II Separation of Boron from seawaterChemical and Petroleum Engineering Department Department Advisor: Dr. Monwar Hussein Examiner committee: Dr. Ali Al-Naqbi Dr. Abdulrahman Al Raisi Dr. Sulaiman Al Zuhair Fall 2010 Ayesha Ibrahim 200514455@uaeu.ac.ae

  2. Agenda • Introduction • Summary of GPI • Unique of the project • Advantages and disadvantages of possible alternatives • Process flow diagram, mass and energy balances • Design of main equipment • Process Economics • Liquid-liquid extraction experiment • Environmental Impact of the Process • HAZOP and Safety Studies • Conclusion • Future of project • Acknowledgments Ayesha Ibrahim 200514455@uaeu.ac.ae

  3. Introduction Problem Statement • Boron concentration in seawater is around 5 mg/L . • World Health Organization (WHO) ruling to be below 0.5 mg/L for drinking water and should not exceed 0.2 mg/L for irrigation. • Separation of boron is very important to be within the recommended limit because of bad effect in health and environment. Ayesha Ibrahim 200514455@uaeu.ac.ae

  4. Introduction Objectives • Select method that will remove boron from seawater without losing that much of essential minerals like: Mg+2, Na+, Cl- and Ca+2. • Design a process that combined between RO and liquid-liquid extraction by using hollow fiber membrane contactor. • Choose non toxic solvent like sunflower oil instead of toxic one which is kerosene. Ayesha Ibrahim 200514455@uaeu.ac.ae

  5. Introduction • Determine main parameters such as area of: RO, membrane contactor and heat exchanger. • Examine the health, safety and HAZOP study in the process • Obtain mass and energy balances for selected design and alternative. • Study the economic analysis to evaluate the designed process. Ayesha Ibrahim 200514455@uaeu.ac.ae

  6. Summary of GPI • Six methods for removing boron from seawater were studied and then liquid-liquid extraction ,ion exchange and reverse osmosis were selected. • The material balance and energy balance were done for the selected methods. Ayesha Ibrahim 200514455@uaeu.ac.ae

  7. Unique of the project • Liquid-liquid extraction process works at natural pH of seawater and normal temperature and pressure. • It can remove 45% of boron in one single stage pass. • The chemicals used in liquid-liquid extraction process are non-toxic and non-corrosive. Ayesha Ibrahim200514455@uaeu.ac.ae

  8. Advantages and disadvantages of possible alternatives Ayesha Ibrahim 200514455@uaeu.ac.ae

  9. Advantages and disadvantages of possible alternatives Ayesha Ibrahim 200514455@uaeu.ac.ae

  10. Process flow diagram Ayesha Ibrahim 200514455@uaeu.ac.ae

  11. Mass balance of two stages of reverse osmosis Assumptions • Steady state. • Recycled system. Basis: • Concentration of boron in= 6 mg/L. • Seawater flowrate= 100 m3/h. Maryam Ali 200508528@uaeu.ac.ae

  12. Mass balance of two stages of reverse osmosis Component material balance for boron in mixing point 1 Drawn by: Maryam Fi: Flowrate of seawater in stream i (m3/h) CBi :Concentration of boron in stream i (mg/L) Maryam Ali 200508528@uaeu.ac.ae

  13. Mass balance of two stages of reverse osmosis Component material balance for boron in RO 1st stage Drawn by: Maryam Maryam Ali 200508528@uaeu.ac.ae

  14. Mass balance of two stages of reverse osmosis Component material balance for boron in RO 2nd stage Drawn by: Maryam Maryam Ali 200508528@uaeu.ac.ae

  15. Mass balance of one stage of reverse osmosis and liquid-liquid extraction Assumption: • Co-current process. • Steady state. Basis: • Boron concentration at seawater feed = 6 mg/L. • Seawater feed flowrate = 100 m3/h. • Reduction in volume in the 1st stage of RO = 20% • Concentration from the 1st stage of RO =1 mg/L • F3= 20 m3/h • CB4= 0 (no boron in solvent) MaryamAli 200508528@uaeu.ac.ae

  16. Mass balance of one stage of reverse osmosis and liquid-liquid extraction Component material balance for boron in RO 1st stage Drawn by: Maryam Fi: Flowrate of seawater in stream i (m3/h) CBi :Concentration of boron in stream i (mg/L) MaryamAli 200508528@uaeu.ac.ae

  17. Component material balance for boron in liquid-liquid extraction Mass balance of one stage of reverse osmosis and liquid-liquid extraction Drawn by: Maryam Maryam Ali 200508528@uaeu.ac.ae

  18. Energy balance on heat exchanger Assumption: • Steady state • No heat loss • Flowrate of seawater = 100 m3/h Basis: • Density of water = 1000 kg/m3 • Flowrate of refrigerant water =50 m3/h MaryamAli 200508528@uaeu.ac.ae

  19. Energy balance on heat exchanger Drawn by: Maryam MaryamAli 200508528@uaeu.ac.ae

  20. Design of main equipment Reverse osmosis membrane design: Data used for performing the calculations: MaryamAli 200508528@uaeu.ac.ae

  21. Design of main equipment Membrane contactor design: MaryamAli 200508528@uaeu.ac.ae

  22. Design of main equipment • Pumps design: • Pretreatment pump: MaryamAli 200508528@uaeu.ac.ae

  23. Design of main equipment • Pumps design: • Reverse osmosis pump: MaryamAli 200508528@uaeu.ac.ae

  24. Heat exchanger design • Aim: cool 100 m3/h of seawater from 30oC to 25oC using refrigerant water at 5oC. • By designing a suitable shell and tube heat exchanger. • Calculation: HaleimahSeraidy 200511109@uaeu.ac.ae

  25. Heat exchanger design Assume: U=1000 watt/m2 .˚C L = 5m Coulson &Richardson’s, Chemical engineering Design, Fourth edition,V.6,P:660-680 HaleimahSeraidy 200511109@uaeu.ac.ae

  26. Heat exchanger design Tube side calculation • All properties were found at average temperature:(Cpavg, ρ, μ, k, pr). • Heat transfer coefficient(hi) was calculated from: Atubes: Cross sectional area of tube (m2) ID: Inner diameter (m) u: Velocity (m/s) Re: Renold number Nu: Nuselt number Pr: Prandelt number hi: Heat transfer coefficient (watt/m2.°C) HaleimahSeraidy 200511109@uaeu.ac.ae

  27. Heat exchanger design Shell side calculation • Calculate the out side heat transfer coefficient HaleimahSeraidy 200511109@uaeu.ac.ae

  28. Heat exchanger design HaleimahSeraidy 200511109@uaeu.ac.ae

  29. Use of HYSIS software packages • HYSIS software was used to verify the heat exchanger calculation: Heat duty and area of heat exchanger. HaleimahSeraidy 200511109@uaeu.ac.ae

  30. Process Economics • It is a well formulated prediction of the probable construction cost of a specific project. • It is any attempt by a company to calculate the price of producing a product before making it. • Types of cost: • Capital Cost • Manufacturing Cost HaleimahSeraidy 200511109@uaeu.ac.ae

  31. Process economics Capital cost HaleimahSeraidy 200511109@uaeu.ac.ae

  32. Process economics • Fixed Manufacturing Cost • Direct Manufacturing Cost • General Expenses Manufacturing Cost Raw material cost HaleimahSeraidy 200511109@uaeu.ac.ae

  33. Process economics Utility Cost HaleimahSeraidy 200511109@uaeu.ac.ae

  34. Process economics Total Manufacturing cost HaleimahSeraidy 200511109@uaeu.ac.ae

  35. Experimental Results • Experiments were done to check whether the desired value of boron reach 0.5 mg/L. • Sunflower oil was used as a solvent which was pumped to shell side where the boron concentration with 1 mg/L was pumped to the tube side • Two runs were done: • First run without diol • Second one with diol as carrier which was better to enhance the extraction Abeer Ahmed 200514464@uaeu.ac.ae

  36. Liquid-liquid extraction experiment Taken by Ayesha Abeer Ahmed 200514464@uaeu.ac.ae

  37. Experimental Results Run1: Sunflower solvent without diol Run2: Sunflower solvent with diol Abeer Ahmed 200514464@uaeu.ac.ae

  38. Experimental Results Results of run1 and run 2 • Using Diol enhance the % removal from 7.51- 45% Abeer Ahmed 200514464@uaeu.ac.ae

  39. Environmental Impact of the Process In our experiment the following chemical were used: • Ethanol :It is used as cleaner of fiber of hollow membranes conductor at start up which is insoluble in water so it doesn't affect. • Sunflower oil: It is used as solvent. It is less toxicity, less corrosiveness, low environmental impact, good health and safety benefits. Abeer Ahmed 200514464@uaeu.ac.ae

  40. HAZOP and Safety Studies • A Hazard and Operability (HAZOP). • Evaluate problems that may represent risks to personnel or equipment, or prevent efficient operation in the plant. • Combinations of parameters (flow, level, pressure and temperature) and guide words (no, more, less) to arise consequences and recommendation. Abeer Ahmed 200514464@uaeu.ac.ae

  41. HAZOP and Safety Studies HAZOP of pump Abeer Ahmed 200514464@uaeu.ac.ae

  42. HAZOP of pump Abeer Ahmed 200514464@uaeu.ac.ae

  43. Conclusions • Concentration of boron in drinking water should be below 0.5 mg/L according to (WHO). • The combination of the RO and liquid-liquid extraction by using hollow fiber membrane contactor represent the selected design • The area of RO, membrane contactor and heat exchanger were equal to 6700 ,5834 and 29 m2 respectively • Capital cost and the manufacturing cost were calculated which equal to $6,306,847 and $3,810,580 respectively. • The main objectives and deliverables of this project are achieved. Abeer Ahmed 200514464@uaeu.ac.ae

  44. Future of project • Doing experiment with high concentration of boron like water production from oil filed(20-25 mg/L). • If high extraction work the RO process it can be eliminate • Treatment of boron from oil phase and get boron as product Abeer Ahmed 200514464@uaeu.ac.ae

  45. Acknowledgments • We would like to express our pleasure and gratitude to: • Our advisor Dr. Md Monwar Hossain. • Faculty coordinate Dr. Ali Al-Naqbi • Training and graduation projects unit. • Family members for their unlimited help and support during our study. Abeer Ahmed 200514464@uaeu.ac.ae

  46. Thank You For Your Attention We will be glad for your questions

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