Senior Design Presentation
Download
1 / 28

Senior Design Presentation Direct Fe Reduction Iron Plant - PowerPoint PPT Presentation


  • 94 Views
  • Uploaded on
  • Presentation posted in: General

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

loader
I am the owner, or an agent authorized to act on behalf of the owner, of the copyrighted work described.
capcha

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.While downloading, if for some reason you are not able to download a presentation, the publisher may have deleted the file from their server.


- - - - - - - - - - - - - - - - - - - - - - - - - - E N D - - - - - - - - - - - - - - - - - - - - - - - - - -

Presentation Transcript


Senior Design PresentationDirect Fe Reduction Iron Plant

Group Golf

Selimos, Blake A.

Arrington, Deisy C.

Sink, Brandon

Ciarlette, Dominic F.

Advisor : OrestRomaniuk

Group Meeting 1 – 01/29/2013


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


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


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


Flow Diagram

5


Flow Diagram - Reformers

6


Flow Diagram – Top Gases

7


Flow Diagram – Feed/Heat Recovery

8


Flow Diagram - Furnace

9


Hand Calculations

Calculating how much H2 will be needed in stream 6

10


Hand Calculations (2)

Calculating how much CH4 will be needed in stream 1

11


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


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


Material Balance

Process Gas (million mol/day)

14


Energy Balance Assumptions

For the furnace temperature we used an average value of 800K.

For the reformer we used a temperature of 1123K

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


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


Energy Balance-Work in progress

Flue Gas heat recovery steam.

Combustion Flue gas provides energy to heat incoming combustion air and feed gas.

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

18


Energy Balance

19


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


Major Equipment Cost

21


Profit

22


Summary

This process will produce 2 million metric tons DRI.

This plant will consume roughly ___ .

23 million mols of CO2 will be sent to the gas treatment plant.

Based on our economic analysis, this plant will cost approximately $______.

23


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


References

25


Questions

26


Complete Flow Diagram

27


28


ad
  • Login