1 / 29

Senior Design Presentation Direct Fe Reduction Iron Plant

Senior Design Presentation Direct Fe Reduction Iron Plant. Group Golf Selimos , Blake A. Arrington, Deisy C. Sink, Brandon Ciarlette , Dominic F . (Scribe) Advisor : Orest Romaniuk Group Meeting 1 – 01/29/2013. Table of Contents. Page 3: Previous Questions Page 4: Design Basis

adolph
Download Presentation

Senior Design Presentation Direct Fe Reduction Iron Plant

An Image/Link below is provided (as is) to download presentation Download Policy: Content on the Website is provided to you AS IS for your information and personal use and may not be sold / licensed / shared on other websites without getting consent from its author. Content is provided to you AS IS for your information and personal use only. Download presentation by click this link. While downloading, if for some reason you are not able to download a presentation, the publisher may have deleted the file from their server. During download, if you can't get a presentation, the file might be deleted by the publisher.

E N D

Presentation Transcript

  1. Senior Design PresentationDirect Fe Reduction Iron Plant Group Golf Selimos, Blake A. Arrington, Deisy C. Sink, Brandon Ciarlette, Dominic F. (Scribe) Advisor : OrestRomaniuk Group Meeting 1 – 01/29/2013

  2. Table of Contents Page 3: Previous Questions Page 4: Design Basis Page 5-9: Process Flow Diagram Page 10-14: Material Balance Page 15-18: Energy Balance Page 19: Work in progress Page 20-22: Economics Page 23: Summary Page 24: Oxy Fuel Booster Page 25: References 2

  3. Previous Questions • Will Sulfur in the methane stream poison the Nickel catalysis? What is our ore source? What is the largest Midrex plant currently in operation? What are our power requirements? 3

  4. Design Basis • 2 million metric tons DRI produced yearly • Receive methane from Gas Treatment Plant • Receive oxygen from Air Separation Plant • Send CO2 to Gas Cleanup Water Reuse Plant 4

  5. Flow Diagram 5

  6. Flow Diagram - Reformers 6

  7. Flow Diagram – Top Gases 7

  8. Flow Diagram – Feed/Heat Recovery 8

  9. Flow Diagram - Furnace 9

  10. Hand Calculations Calculating how much H2 will be needed in stream 6 10

  11. Hand Calculations (2) Calculating how much CH4 will be needed in stream 1 11

  12. Material Balance Assumptions • Post reformer • Assume following conversion rates • Reaction 1: 80% • Reaction 2: 80% • Reaction 3: 80% • Post OXY booster • Assume booster adds 5.0% of stream 5 to stream 5. • Assume conversion rate of 80% • Post shaft furnace • Assume reduction reaction conversion rates of 93% • Process gas split • Assume all steam is condensed and all water is sent to process recycle stream. • Assume 60:40 split for streams 9:17. 12

  13. Material Balance Assumptions (2) • Post CO2 removal • Assume 100% removal of appreciable CO2. • Top gas to combustion split • Assume no water in this stream. • Ore feed • Assume only Fe2O3. • In reality this stream will contain, in addition to Fe2O3, Fe3O4, and SiO2. • Needs to be corrected to include other components. • Product stream • Assume only pure Fe and residual Fe2O3. • Post reformer combustion • Assume total combustion of fuel gases from stream 21. 13

  14. Material Balance Process Gas (million mol/day) 14

  15. Energy Balance Assumptions For the furnace temperature we used an average value of 980F. For the reformer we used a temperature of 1562F Energy balance of furnace based only on incoming and outgoing iron due to weight of iron being substantially higher than weight of incoming gases. 15

  16. Energy Balance Page 5-6: Process Flow Diagram (1) Page 7-12: Material Balance Page 13-15: Energy Balance Page 16: Work in progress Page 17-19: Economics Page 20: Summary Page 21: References Page 23: Process Flow Diagram (2) 16

  17. Energy Hand Calculations Endothermic Reaction in the Primary Reformer CH4+ CO2 → 2CO + 2H2 ΣH°f=(2*-95038693.04)+(2*0)-(-64075666.38)-(-338357695.6) ΣH°f= 40,729,381 (h2-h1)CH4=0.03431(850-25)+(8502-252)+ (8503-503)+*(8504-504) (h2-h1)CH4=212,355,976 ∆H=212355976+(2*22191541)+(2*20967220)-40729381-44680237 ∆H=213,263,879.8 17

  18. Energy Balance 18

  19. Energy Balance-Work in progress Flue Gas heat recovery steam. Combustion Flue gas provides energy to heat incoming combustion air and feed gas. 19

  20. Total Capital Investment Page 5-6: Process Flow Diagram (1) Page 7-12: Material Balance Page 13-15: Energy Balance Page 16: Work in progress Page 17-19: Economics Page 20: Summary Page 21: References Page 23: Process Flow Diagram (2) 20

  21. Major Equipment Cost 21

  22. Profit 22

  23. Summary This process will produce 2.2 million tons DRI. This plant will consume roughly 210,000 MW-h annually. 23 million mols of CO2 will be sent to the gas treatment plant. Based on our economic analysis, this plant will cost approximately $97 million. 23

  24. Oxygen-Fuel Boost Reformer Relatively new technology for secondary oxygen reforming in MidrexProcesses. Uses a two step partial combustion process in which oxygen and methane are mixed and combusted in the first stage. The combustion gases are then mixed in an elongated mixing tube with methane and oxygen in a swirling motion producing H2 on CO syngas along with H2O, CO2 and CH4 to be used as enrichment gases to combine with and enhance the reducing gas from the reformer. This increases the reducing gas amount and temperature of gas going to the furnace increasing productivity. 24

  25. References • http://www.midrex.com/uploads/documents/MIDREXShaftBrochure2.pdf • http://www.midrex.com/uploads/documents/MidrexCorporateBrochure1.pdf • US patent # 6602317 b2 • US patent # 6524356 b2 • US patent # 6506230 b2 • http://www./handler.cfm/cat_id/163/section/global • http://www.midrex.com/uploads/documents/SSS.pdf • http://www.midrex.com/uploads/documents/DFM1Q041.pdf • http://www.midrex.com/uploads/documents/New%20Developments%20in%20the%20Midrex%20DR%20Process.pdf 25

  26. Questions 26

  27. Complete Flow Diagram 27

  28. 28

More Related