![28 t/hr
NH3
109 t/hr
HNO3
18 t/hr NH3
[t/hr] = tonne/hour
109 t/hr
60% Nitric Acid
1](data:image/gif;base64,R0lGODlhAQABAIAAAAAAAP///yH5BAEAAAAALAAAAAABAAEAAAIBRAA7)
Recommended
More Related Content
What's hot
What's hot (20)
Similar to Nitric Acid Production Plant
Similar to Nitric Acid Production Plant (20)
Recently uploaded
Recently uploaded (20)
Nitric Acid Production Plant
- 2. 28 t/hr NH3 109 t/hr HNO3 18 t/hr NH3 [t/hr] = tonne/hour 109 t/hr 60% Nitric Acid 1
- 3. Overview Control Design Safety Energy Economics Next Step Sulfuric Acid Phosphoric Acid Ammonia NPK DAP Excess Ammonia Water Air Hydrocarbon Water Phosphate Rock Sulphur Air 2
- 4. Overview Control Design Safety Energy Economics Next Step Sulfuric Acid Phosphoric Acid Ammonia NPK DAP Nitric Acid Ammonium Nitrate Projected Production Chain Water Air Water Air Hydrocarbon Water Phosphate Rock Sulphur Air 2
- 5. Overview Control Design Safety Energy Economics Next Step Ammonia Plant 46 t/hr Ammonium Nitrate Plant 18 t/hr Out of Scope Nitric Acid Plant 28t/hr Nitric Acid Production 23.5 t/hr Flue Gas Treatment 4.5 t/hr 3
- 6. Overview Control Design Safety Energy Economics Next Step 4
- 7. Overview Control Design Safety Energy Economics Next Step 5
- 8. Overview Control Design Safety Energy Economics Next Step 5
- 9. Overview Control Design Safety Energy Economics Next Step 5
- 10. Overview Control Design Safety Energy Economics Next Step Catalytic Reactor NO Oxidation Absorption Tower 6
- 11. Overview Control Design Safety Energy Economics Next Step 7
- 12. (62 MPPH) Overview Control Design Safety Energy Economics Next Step Humid Air (352 t/hr) Condensate (109 t/hr) Dry Air (57 t/hr) Ammonia (28 t/hr) Ammonia (4.5 t/hr) 8
- 13. Overview Control Design Safety Energy Economics Next Step Demin Water (163 t/hr) Condensate (55 t/hr) High Pressure Steam (108 t/hr) 9 198β β 980β β 150β
- 14. Oxygen (22 t/hr) Overview Control Design Safety Energy Economics Next Step 10 310 πππ β 500 πππ
- 15. Overview Control Design Safety Energy Economics Next Step Demin Water (14 t/hr) 60% Nitric Acid (109 t/hr) 11
- 16. Overview Control Design Safety Energy Economics Next Step Ammonia (4.5 t/hr) Treated Flue Gas (235 t/hr) 12
- 17. (62 MPPH) 60% Nitric Acid (109 t/hr) Ammonia (28 t/hr) Ammonia (4.5 t/hr) Air (352 t/hr) Condensate (109 t/hr) Dry Air (57 t/hr) O2 (22 t/hr) Demin Water (14 t/hr) Overview Control Design Safety Energy Economics Next Step 13
- 18. Overview Control Design Safety Energy Economics Next Step 14
- 19. Overview Control Design Safety Energy Economics Next Step 14
- 20. Overview Control Design Safety Energy Economics Next Step 14
- 21. Overview Control Design Safety Energy Economics Next Step 14
- 22. Overview Control Design Safety Energy Economics Next Step 14
- 23. Overview Control Design Safety Energy Economics Next Step 15
- 24. Overview Control Design Safety Energy Economics Next Step Spring Disc Nozzle Sized for Exterior fire 16
- 25. Overview Control Design Safety Energy Economics Next Step Spring Disc Nozzle Sized for Exterior fire MAWP* 725 kPa Relief Pressure 979 kPa Allowable Overpressure 189 kPa *MAWP = Maximum allowable working pressure 16
- 26. [ ] Overview Control Design Safety Energy Economics Next Step Spring Disc Nozzle Sized for Exterior fire MAWP* 725 kPa Relief Pressure 979 kPa Allowable Overpressure 189 kPa 3 P-Type PSVs in Parallel 16
- 27. Overview Control Design Safety Energy Economics Next Step Nozzle Description Pipe Diameter [mm] N1 Gaseous NO Outlet 1328 N2 NH3/Air Inlet 1625 N3 Manhole 610 Shallow Bed Reactor 17
- 28. Overview Control Design Safety Energy Economics Next Step Nozzle Description Pipe Diameter [mm] N1 Gaseous NO Outlet 1328 N2 NH3/Air Inlet 1625 N3 Manhole 610 Shallow Bed Reactor Design Pressure 538 kPa Design Temperature 1093 Β°C *MOC SS 347 Catalyst Platinum-10% Rhodium *MOC = Material of Construction 17
- 29. Overview Control Design Safety Energy Economics Next Step Nozzle Description Pipe Diameter [mm] N1 Gaseous NO Outlet 1328 N2 NH3/Air Inlet 1625 N3 Manhole 610 Shallow Bed Reactor Design Pressure 538 kPa Design Temperature 1093 Β°C *MOC SS 347 Catalyst Platinum-10% Rhodium *MOC = Material of Construction 17
- 30. Overview Control Design Safety Energy Economics Next Step Nozzle Description Pipe Diameter [mm] N1 Gaseous NO Outlet 1328 N2 NH3/Air Inlet 1625 N3 Manhole 610 Shallow Bed Reactor Design Pressure 538 kPa Design Temperature 1093 Β°C *MOC SS 347 Catalyst Platinum-10% Rhodium *MOC = Material of Construction 17
- 31. Overview Control Design Safety Energy Economics Next Step Nozzle Description Pipe Diameter [mm] N1 Gaseous NO Outlet 1328 N2 NH3/Air Inlet 1625 N3 Manhole 610 Shallow Bed Reactor Design Pressure 538 kPa Design Temperature 1093 Β°C *MOC SS 347 Catalyst Platinum-10% Rhodium *MOC = Material of Construction 17
- 32. Number of gauzes needed 28 Height of catalyst bed 4.3 cm Volume of catalyst bed 0.51 m3 Catalyst Bed Design Overview Control Design Safety Energy Economics Next Step 18
- 33. Number of gauzes needed 28 Height of catalyst bed 4.3 cm Volume of catalyst bed 0.51 m3 Catalyst Bed Design Overview Control Design Safety Energy Economics Next Step 18
- 34. Number of gauzes needed 28 Height of catalyst bed 4.3 cm Volume of catalyst bed 0.51 m3 Catalyst Bed Design Overview Control Design Safety Energy Economics Next Step 18
- 35. Number of gauzes needed 28 Height of catalyst bed 4.3 cm Volume of catalyst bed 0.51 m3 Catalyst Bed Design Overview Control Design Safety Energy Economics Next Step Reactor Design Diameter of reactor 4.3 m Volume of reactor 87.0 m3 Height of reactor 6.1 m 18
- 36. Number of gauzes needed 28 Height of catalyst bed 4.3 cm Volume of catalyst bed 0.51 m3 Catalyst Bed Design Overview Control Design Safety Energy Economics Next Step Reactor Design Diameter of reactor 4.3 m Height of reactor 6.1 m Volume of reactor 87.0 m3 18
- 37. Number of gauzes needed 28 Height of catalyst bed 4.3 cm Volume of catalyst bed 0.51 m3 Catalyst Bed Design Overview Control Design Safety Energy Economics Next Step Reactor Design Diameter of reactor 4.3 m Height of reactor 6.1 m Volume of reactor 87.0 m3 18
- 38. Addition of a waste-heat recovery system Recommendations Addition of a gas inlet distributor Overview Control Design Safety Energy Economics Next Step 19
- 39. Overview Control Design Safety Energy Economics Next Step 20 2 km 4.2 km
- 40. Catalytic Ammonia Oxidation HPS Flow 108 t/hr Steam Generation 1 2 3 High Pressure Steam (HPS) WHB Demin WaterHPS NO Overview Control Design Safety Energy Economics Next Step 21
- 41. NO Oxidation LPS Flow 78 t/hr Steam Generation 3 Low Pressure Steam (LPS) WHB Demin WaterLPS NO 1 2 O2 Overview Control Design Safety Energy Economics Next Step 22
- 42. Flue Gas Treatment MPS Flow 34 t/hr Steam Generation 2 Medium Pressure Steam (MPS) WHB Demin WaterMPS Flue Gas 1 3 SCR Overview Control Design Safety Energy Economics Next Step 23
- 43. Steam Generation HPS LPS MPS 108 t/hr 78 t/hr 34 t/hr [ ] Total Power from Steam 55.7 GWh* Overview Control Design Safety Energy Economics Next Step *on a per 330 day basis 24
- 44. Turbine Generation Overview Control Design Safety Energy Economics Next Step *on a per 330 day basis Absorption Tower NO Power 18.4 GWh Flue Gas Treatment Power 54.2 GWh 25
- 45. Turbine Generation Absorption Tower Flue Gas Treatment 108 t/hr 78 t/hr [ ]Total Power from Turbines 72.6 GWh* Overview Control Design Safety Energy Economics Next Step *on a per 330 day basis 26
- 46. Overview Control Design Safety Energy Economics Next Step Input Energy 216 GWh* *on a per 330 day basis 27
- 47. Overview Control Design Safety Energy Economics Next Step Input Energy 216 GWh* 60% 129 GWh* Recovered Energy *on a per 330 day basis 27
- 48. Overview Control Design Safety Energy Economics Next Step Recovered Energy Net Energy Requirements 88 GWh* Input Energy 216 GWh* 60% 129 GWh* 7500 *on a per 330 day basis 27
- 49. [ ] Overview Control Design Safety Energy Economics Next Step Recovered Energy Net Energy Requirements 365 kJ/kg Input Energy 216 GWh* 60% 129 GWh* *on a per 330 day basis 27 88 GWh* 7500
- 50. Overview Control Design Safety Energy Economics Next Step 28
- 51. TCI $301M Direct Costs $186M Indirect Costs $55M Working Capital $60M Overview Control Design Safety Energy Economics Next Step 28
- 52. TPC $173M/yr Direct Production Costs $159M/yr Fixed Charges $7.2M/yr General Expenses $7.4M/yr Overview Control Design Safety Energy Economics Next Step 29
- 53. Overview Control Design Safety Energy Economics Next Step Direct Production Costs $159M/yr Raw Materials $112M/yr Utilities $32M/yr Other $15M/yr 29
- 54. -$250.00 -$200.00 -$150.00 -$100.00 -$50.00 $0.00 $50.00 $100.00 $150.00 $200.00 $250.00 $300.00 0 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 CashFlow[$millionUSD] Time [years] Net Present Value Net Profit After Tax $78M/yr Net Present Value $274M Payback Period 5.5 years Internal Rate of Return 26% Return on Investment 91% 30
- 55. Criteria Worst Case Scenario Best Case Scenario Average Scenario Random Profit over 20 years $51M USD $135M USD $101 Net Present Value (NPV) $51M USD $594M USD $375M USD Overview Control Design Safety Energy Economics Next Step 31
- 56. Overview Control Design Safety Energy Economics Next Step 32
- 57. Overview Control Design Safety Energy Economics Next Step 1 2 3 Integrated Heat Recovery 33
- 58. Overview Control Design Safety Energy Economics Next Step 1 2 3 Integrated Heat Recovery WHB WaterHPS 33
- 59. Overview Control Design Safety Energy Economics Next Step 1 2 3 Integrated Heat Recovery Catalytic reactor with integrated waste heat boiler WHB Water HPS WaterHPS 34
- 60. Overview Control Design Safety Energy Economics Next Step 2 Integrated Energy Recovery Integrated Heat Recovery 3 1 35
- 61. Overview Control Design Safety Energy Economics Next Step 2 Integrated Energy Recovery 3 1 Designed 35
- 62. Overview Control Design Safety Energy Economics Next Step 2 Integrated Energy Recovery 3 1 Designed 35
- 63. Overview Control Design Safety Energy Economics Next Step 2 Integrated Energy Recovery 3 1 Designed Suggested MAN Diesel & Turbo 35
- 64. Overview Control Design Safety Energy Economics Next Step 3 Integrated Energy Recovery Integrated Heat Recovery Optimization of Utilities 1 2 36
- 67. Criteria Definition Plant Capacity [MPPH] Maximum plant capacity in terms of nitric acid production flow (100% basis) Nitric Acid Yield [%] Actual plant yield over theoretical yield Catalyst Loss Unrecoverable loss of the platinum catalyst Maintenance Frequency Frequency of localized shutdown of the plant NOx Emission [ppm] Concentration of NO, NO2 in the flue gas Electric Power [HP] Electric power consumption per day at 100% plant capacity Capital Cost [US $] Purchase cost of main equipments
- 68. Type Pressure (kPa) Temperature (β) High Pressure Steam 4826 276 Medium Pressure Steam 483 169 Low Pressure Steam 276 149
- 69. Mesh size 203 cm-1 Wire diameter 0.08 In Porosity 0.806 - Number of gauzes needed 28 Height of catalyst bed 4.3 cm Diameter of catalyst bed 3.9 m Weight of catalyst and gauzes 484 kg Volume of catalyst bed 0.51 m3 Catalyst Bed Design Overview Control Design Safety Energy Economics Next Step
- 70. Reactor Design Design temperature 1093 Β°C Design pressure 538 kPa Diameter of reactor 4.3 m Volume of reactor 87.0 m3 Height of reactor 6.1 m MOC SS 347 - Type of head Dished heads - Shell thickness 1.0 cm Head thickness 1.4 cm Vessel weight 9134 kg Total weight 9618 kg Overview Control Design Safety Energy Economics Next Step
- 73. Criteria Worst Case Scenario Best Case Scenario Average Scenario Average Random Profit over 20 years $51M USD $135M USD $101 Net Present Value (NPV) $51M USD $594M USD $375M USD Internal Rate of Return (IRR) 14% 41% 30% Return on Investment (ROI) 18% 197% 125% Overview Control Design Safety Energy Economics Next Step
- 78. 78
- 79. 79
- 80. 80
- 81. 81
- 82. 82
- 83. 83
- 84. 84
- 85. 85
- 86. 86
- 87. 87
- 88. 88