NITRIC ACID PLANT (63% wt. HNO3) Ammonia-Based Fertilizers University of Illinois at Chicago Department of Chemical Engineering CHE 397 Senior Design II January 24, 2012 Thomas Calabrese (Team Leader) Cory Listner Hakan Somuncu (Scribe) David Sonna Kelly Zenger 1 Today’s Agenda Big Picture – Fertilizer Plant Supplier Customers Nitric Acid Plant Design Basis Starting Reagents Products Environmental Concerns Process Block Flow Diagram General Process Overview Catalysts Useful Energy Recovery Pressure and Temperature Effects NOx Emission Control 2 BIG PICTURE-FERTILIZER PLANT Ammonia (Liquid) Supplier (603.5 TPD) INTERNAL AIR (10820 TPD) CUSTOMER 2571.2 TPD HNO3 (63 wt%) OUTSIDE CUSTOMERS 717.8 TPD HNO3 (63 wt%) 3 Design Basis Produce 3,289 TPD of 63% wt. nitric acid solution (~14M) Starting Reagents Ammonia (NH3) - 603.5 TPD Excess Air – 10,819.5 TPD Excess Oxygen (O2) from Air – 2,272.0 TPD Products 63% wt. Nitric Acid Solution (HNO3) - 3,289.0 TPD Water (H2O) – 1,216.9 TPD Useful Heat Environmental Concerns Oxides of Nitrogen (NOx) (<200 ppm) Nitrous Oxide (N2O) (<200 ppm) 4 572 TPD NH3 (g) from Ammonia Plant Ammonia Filtration Mixing Catalytic Reactor (Oxidation of NH3) NO (g) 10,322 TPD Air Air Filtration Air Compression Heat Recovery (Oxidation of NO) 1,843 TPD Steam to CHP Atmosphere Gas Expander Nox Compressor Hot Tail Gas NOx (g) NO2 (g) Bleacher Column Absorption Column (Strip Dissolved NOx) (Formation of HNO3) 607 TPD Process Water Cold Tail Gas 3,289 TPD 63% wt. HNO3 718 TPD to Market 2,571 TPD to Ammonium Nitrate General Process Overview Primary Chemical Reactions (Ostwald Process) Oxidation of Ammonia to Nitrogen Monoxide 4NH3 (g) + 5O2 (g) 4NO (g) + 6H2O (g) Oxidation of Nitric Oxide to Nitrogen Dioxide 2NO (g) + O2 (g) 2NO2 (g) Reaction of Nitrogen Dioxide to Nitric Acid 3NO2 (g) + H2O (l) 2HNO3 (aq) + NO (g) Side Chemical Reactions Simultaneous to Oxidation of Ammonia 4NH3 (g) + 3O2 (g) 2N2 (g) + 6H2O (g) 4NH3 (g) + 4O2 (g) 2N2O (g) + 6H2O (g) 6 Materials of Construction Material Pros Cons Steel and aluminum Cheap, can be used at low temperatures At elevated temperatures forms oxides and nitride films on surface of metal. Stainless Steel Operating performance, less maintenance. Required for elevated temperatures. Corrosion resistant. Higher capital cost compared to basic metals Hastelloy (Nickel alloy) Highly corrosion resistant. Can be operated at high temperature and high stress More expensive than stainless steel. Degradation due to handling. Monel (Nickel Alloy) Can be operated at high temperatures. Corrosion resistant Much more expensive than stainless steel 7 Energy Recovery Methods Heat from Oxidation in Catalytic Reactor Heat from Absorption Mechanical Energy from Tail Gas Expansion 8 Energy Recovery Methods Net Energy Exporter Little effect from single/dual-pressure and other considerations Steam (standard) Oxidation reaction: 1,600 Btu/lb of pure nitric acid Absorption process: 370 Btu/lb Tail gas turbine: 325 Btu/lb (~80% of mechanical energy used) Total: 1,955 Btu/lb (967-1,217 Btu/lb at 50-65% efficiency) Augmented with natural gas at startup Combined Heat & Power (CHP) Generate high pressure steam and run through turbine Offsets power purchase from the grid 9 Which Catalyst? Platinum-Rhodium Cobalt Oxide (Co3O4) Cost ($/short ton $3 - $4 of HNO3 produced) $0.50 - $0.75 Lifespan 3-4 months 12 months Downtime 4 hours to replace gauze at end of lifespan Remove Rhodium Oxide buildup (every 3-4 weeks) None Conversion Efficiency 93% - 96% 95% - 98% Operating Parameters 24-95 psi, 1490-1724 °F 0-95 psi, 1549 °F Use Very common, industry standard New, commercial use Drawbacks Cost, lifespan, and greater N2O formation Minimal data available, new reactor design, deactivation to CoO 10 Why are Pressure and Temperature Important? Cost Catalyst Life NH3 Oxidation NO Oxidation Absorption of NO2 Low Pressure (0-25 psig) Lowest Cost Shorter than Dual Increased Oxidation Rate Decreased Yield Less Absorption High Pressure (90-120 psig) Increased Cost Shorter than Dual Reduced Oxidation Rate Increased Yield Improved Absorption Dual Pressure Highest Capital and Materials Cost Longest Catalyst Life Increased Oxidation Rate, Best Conversion Increased Yield Improved Absorption Increased Temperature - - Increased Yield Decreased Yield Improved Absorption 11 Controlling NOx Release Primary Methods-reduce N2O formed during ammonia oxidation 70-85% efficiency Add an “empty” reaction chamber between the catalyst bed and the first heat exchanger (increase residence time) Modify the catalyst used during the ammonia oxidation Secondary Methods-reduce N2O formed immediately after ammonia oxidation (Selective Catalytic Reduction) Up to 90% efficiency Secondary catalyst is used to promote N2O decomposition by increasing the residence time in the ammonia burner 2N2O (g) 2N2 (g) + O2 (g) 12 Controlling NOx Release Tertiary Methods-reduce N2O from or to the tail gas (Non-Selective Catalytic Reduction) 80-98+% efficiency A reagent fuel (e.g. H2 from an ammonia plant purge) is used over a catalyst to produce N2 and water Alternatively, following SCR the tail gas is mixed with ammonia and reacts over a second catalyst bed to give N2 and water 13 Thermodynamic Models for HNO3 (63 wt%) Plant Up-stream of HNO3 (63 wt%) Plant – Soave-Redlich-Kwong (SRK) The SRK property method uses the Soave-Redlich-Kwong (SRK) cubic equation of state for all thermodynamic properties with option to improve liquid molar volume Mixture Types Use the SRK property method for non-polar or mildly polar mixtures. This property method is particularly suitable in the high temperature and high pressure regions Range It can be expected reasonable results at all temperatures and pressures. The SRK property method is consistent in the critical region. Therefore, unlike the activity coefficient property methods, it does not exhibit anomalous behavior. Results are least accurate in the region near the mixture critical point. Down-stream of HNO3 (63 wt%) Plant - ELECNRTL It can handle very low and very high concentrations It can handle aqueous and mixed solvent systems The solubility of supercritical gases can be modeled using Henry ‘s Law The Redlich-Kwong equation of state is used for all vapor phase properties Mixture Types Any liquid electrolyte solution unless there is association in the vapor phase Range Vapor phase properties are described accurately up to medium pressures. Aspen Database Summary Produce 3,289 TPD of 63% wt. Nitric Acid Key Equipment Ammonia Evaporator, Air Compressor, Catalytic Reactor, and Absorption Column Competing Processes Platinum-Rhodium Alloy or Cobalt Oxide Single or Dual Pressure System Energy Recovery Materials of Construction 15 Looking Ahead Problem areas to be addressed Catalyst decision Single or dual pressure plant decision Material balance Thermodynamic model Method of pollution control Equipment material Finalized Material and Energy Balances Rough Economics Hand Calculations Additions to Report 16 References ASPEN Thermodynamic Database. Available and Emerging Technologies for Reducing Greenhouse Gas Emissions from the Nitric Acid Production Industry. U.S. Environmental Protection Agency. 2010. <http://www.epa.gov/nsr/ghgdocs/nitricacid.pdf>. Bell, B. Platinum Catalysts in Ammonia Oxidation. Platinum Metals Rev. 4. 1960. Best Available Techniques for Pollution Prevention and Control in the European Fertilizer Industry, Production of Nitric Acid. EFMA. 2000. <http://www.efma.org/PRODUCT-STEWARDSHIPPROGRAM-10/images/EFMABATNIT.pdf>. Cobalt Oxide Catalyst. Catalyst Development Corporation. 2003. <http://www.cobaltoxide.com/>. Pratt, Christopher, and Robert Noyes. Nitrogen Fertilizer Chemical Processes. Pearl River: 1965. Ullman’s Encyclopedia of Industrial Chemistry. Volume A17. VCH. 17 Questions? 18
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