Large Volume Inorganic Chemicals - Ammonia ... - ammk-rks.net
Large Volume Inorganic Chemicals - Ammonia ... - ammk-rks.net Large Volume Inorganic Chemicals - Ammonia ... - ammk-rks.net
Chapter 4Achieved environmental benefitsNote: Conversion rates, tail gas SO 2 concentrations and specific SO 2 load in tail gases arecorrelated, see Figure 4.7, Figure 4.8 and Figure 4.9.Average daily conversion rates of at least 99.7 – 99.9 % with double contact processes [154,TWG on LVIC-AAF]. Conversion rates of 99.8 % are achievable with four catalyst beds andinlet gas of low variabilility. With four catalyst beds and inlet gases from non-ferrous metalproduction (higher variability), 99.7 % are achievable [57, Austrian UBA, 2001]. For examplesof degree of variation of the SO 2 inlet concentration and the variation of the conversion rate, seeFigure 4.12 and Figure 4.13.For energy recovery and export, see Section 4.4.15.99,914Conversion rate in %99,8599,899,75Conversionrate in %SO 2 inlet concentrationin % v/v131211109SO2 inlet cioncentration in % v/v99,724 hours of operation8Figure 4.12: SO 2 inlet concentration and conversion rate of production based on sulphur burning[154, TWG on LVIC-AAF, 2006]99,8012,099,7511,5Conversion rate in %99,7099,6599,6099,5599,5099,4599,4099,3599,30Conversionrate in %SO 2 inletconcentrationin % v/v11,010,510,09,59,08,58,07,57,0SO2 inlet concentration in % v/v24 hours of operationFigure 4.13: SO 2 inlet concentration and conversion rate of production based on Zn roasting[154, TWG on LVIC-AAF, 2006]174 Large Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers
Chapter 4Cross-media effectsNone believed likely.Operational dataIn general, the process uses gases with an SO 2 content of 10 to 11 % [58, TAK-S, 2003]. Theinlet gas temperature is about 400 ºC. Gases with lower temperatures, e.g. metallurgical gasesafter purification, require reheating from 50 to 400 ºC. This is usually carried out with recoveredheat from the conversion process [57, Austrian UBA, 2001].Applicability• applicable for SO 2 inlet content of 5 – 12 % v/v [58, TAK-S, 2003]• applicable for SO 2 inlet content of >4.5 up to 14 % v/v. Below 4.5 % v/v, double contactprocesses do not work autothermally [59, Outukumpu, 2005].Pressure contact process. One plant is known to operate a double contact process at an elevatedpressure of 5 bar. This increases the conversion rate by shifting the conversion equilibrium andfavouring the formation of SO 3 . The pressure double contact process achieves 99.8 – 99.85 %conversion; here, the tail gas contains 200 – 250 ppm SO 2 . The disadvantages are higherelectricity consumption and, at the same time, less steam production. Higher NO x emissions arecaused by higher sulphur combustion temperatures (1800 ºC). In comparison, savings of 10 – 17% on investment costs are gained. However, the benefits from building a plant for smaller gasvolumes (at higher pressure) are offset by more stringent safety regulations and additional costsfor pressure resistant materials.EconomicsThe double contact/double absorption process is considered as the baseline for inlet gas SO 2concentrations >4.5 % v/v.Driving force for implementationDevelopment of the single contact/single absorption process.References to literature and example plants[57, Austrian UBA, 2001, 58, TAK-S, 2003], Donau Chemie AG, Lenzing AG, Degussa AGLarge Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers 175
- Page 151 and 152: Chapter 33.4.6 Catalytic N 2 O deco
- Page 153 and 154: Chapter 3According to [89, Kuiper,
- Page 155 and 156: Chapter 33.4.7 Combined NO x and N
- Page 157 and 158: Chapter 3EconomicsInvestment costs.
- Page 159 and 160: Chapter 3Operational dataSee descri
- Page 161 and 162: Chapter 3NOx removal efficiency in
- Page 163 and 164: Chapter 33.4.10 Addition of H 2 O 2
- Page 165 and 166: Chapter 33.4.11 NO X reduction duri
- Page 167 and 168: Chapter 3Installing a low temperatu
- Page 169 and 170: Chapter 3NO x emission level as NO
- Page 171: Chapter 3Operational dataNo specifi
- Page 174 and 175: Chapter 4Country Company Location C
- Page 176 and 177: Chapter 4Country Company Location C
- Page 178 and 179: Chapter 4Figure 4.2 gives an overvi
- Page 180 and 181: Chapter 4Two general converter type
- Page 182 and 183: Chapter 4Figure 4.6 gives an impres
- Page 184 and 185: Chapter 44.2.3 Sulphur sources and
- Page 186 and 187: Chapter 44.2.3.5 Non-ferrous metal
- Page 188 and 189: Chapter 4Sulphur source/SO 2 produc
- Page 190 and 191: Chapter 44.3 Current emission and c
- Page 192 and 193: Chapter 410Tail gas specific SO2 lo
- Page 194 and 195: Chapter 4Capacity in tonnesof 100 %
- Page 196 and 197: Chapter 4Capacity in tonnesof 100 %
- Page 198 and 199: Chapter 4SO 2 sourceSpent acid and
- Page 200 and 201: Chapter 4Cross-media effectsWithout
- Page 204 and 205: Chapter 44.4.3 Addition of a 5 th b
- Page 206 and 207: Chapter 44.4.4 Application of a Cs-
- Page 208 and 209: Chapter 4EUR/yearWaste gas volume (
- Page 210 and 211: Chapter 44.4.6 Replacement of brick
- Page 212 and 213: Chapter 4EUR/yearWaste gas volume (
- Page 214 and 215: Chapter 4PlantSO 2 sourceInlet SO 2
- Page 216 and 217: Chapter 44.4.10 Combination of SCR
- Page 218 and 219: Chapter 4Achieved environmental ben
- Page 220 and 221: Chapter 4Driving force for implemen
- Page 222 and 223: Chapter 44.4.14 Monitoring of SO 2
- Page 224 and 225: Chapter 4EconomicsCost benefits can
- Page 226 and 227: Chapter 4Energy inputRecovery and l
- Page 228 and 229: Chapter 44.4.16 Minimisation and ab
- Page 230 and 231: Chapter 44.4.17 Minimisation of NO
- Page 232 and 233: Chapter 44.4.19 Tail gas scrubbing
- Page 234 and 235: Chapter 44.4.21 Tail gas treatment:
- Page 236 and 237: Chapter 4Economics[58, TAK-S, 2003]
- Page 238 and 239: Chapter 4EconomicsNo specific infor
- Page 240 and 241: Chapter 4BAT is to minimise and red
- Page 242 and 243: Chapter 55.2 Applied processes and
- Page 244 and 245: Chapter 55.2.2.1 Raw materials5.2.2
- Page 246 and 247: Chapter 5OriginChinaMine/regionRare
- Page 248 and 249: Chapter 55.2.2.2 GrindingDepending
- Page 250 and 251: Chapter 55.3 Current emission and c
Chapter 4Cross-media effectsNone believed likely.Operational dataIn general, the process uses gases with an SO 2 content of 10 to 11 % [58, TAK-S, 2003]. Theinlet gas temperature is about 400 ºC. Gases with lower temperatures, e.g. metallurgical gasesafter purification, require reheating from 50 to 400 ºC. This is usually carried out with recoveredheat from the conversion process [57, Austrian UBA, 2001].Applicability• applicable for SO 2 inlet content of 5 – 12 % v/v [58, TAK-S, 2003]• applicable for SO 2 inlet content of >4.5 up to 14 % v/v. Below 4.5 % v/v, double contactprocesses do not work autothermally [59, Outukumpu, 2005].Pressure contact process. One plant is known to operate a double contact process at an elevatedpressure of 5 bar. This increases the conversion rate by shifting the conversion equilibrium andfavouring the formation of SO 3 . The pressure double contact process achieves 99.8 – 99.85 %conversion; here, the tail gas contains 200 – 250 ppm SO 2 . The disadvantages are higherelectricity consumption and, at the same time, less steam production. Higher NO x emissions arecaused by higher sulphur combustion temperatures (1800 ºC). In comparison, savings of 10 – 17% on investment costs are gained. However, the benefits from building a plant for smaller gasvolumes (at higher pressure) are offset by more stringent safety regulations and additional costsfor pressure resistant materials.EconomicsThe double contact/double absorption process is considered as the baseline for inlet gas SO 2concentrations >4.5 % v/v.Driving force for implementationDevelopment of the single contact/single absorption process.References to literature and example plants[57, Austrian UBA, 2001, 58, TAK-S, 2003], Donau Chemie AG, Lenzing AG, Degussa AG<strong>Large</strong> <strong>Volume</strong> <strong>Inorganic</strong> <strong>Chemicals</strong> – <strong>Ammonia</strong>, Acids and Fertilisers 175