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Chapter 4Economics[58, TAK-S, 2003] estimates the additional yearly costs for applying an H 2 O 2 scrubber after thefinal absorber of a single contact plant as follows (basis: 1000 tonnes H 2 SO 4 /day, removal of 10tonnes SO 2 per day):Total costs: EUR 1965000.This includes costs for personnel, depreciation, maintenance, electric power and raw materials.Driving force for implementationLower SO 2 emission levels.References to literature and example plants[57, Austrian UBA, 2001, 58, TAK-S, 2003, 62, EFMA, 2000, 63, Laursen, 2005], RöhmGmbH Wesseling, Kemira Kemi Helsingborg (in combination with a 5 th bed), Lenzing AG,Newmont Gold (USA), CPM (Brazil)208 Large Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers
Chapter 44.4.23 Removal of Hg from process gasesDescriptionAcids produced in smelting processes or from recycling plants may contain mercury. Most ofthe mercury passes into the sulphuric acid plant with the process gas which contains SO 2 and, ifit is not washed out through the washing and cooling plant, it will end up in the sulphuric acidproduct. Besides removal of mercury from the product acid (see Table 4.6), mercury can beremoved from process gases. Table 4.23 gives an overview.MethodBoliden-Norzink method(Kalomel)Outokumpu methodDOWA methodSodium thiocyanatemethodSpecial conditionsGas scrubbing with a solution containing Hg 2+with formation of Hg 2 Cl 2
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EUROPEAN COMMISSIONIntegrated Pollu
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Executive SummaryEXECUTIVE SUMMARYT
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Executive SummaryII.Production and
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Executive Summarybed, using a cesiu
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Executive SummaryConversion process
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Executive SummaryBAT is to treat al
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PrefacePREFACE1. Status of this doc
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Preface5. How to understand and use
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2.2.4.2 Gasification of heavy hydro
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5.4.2 Hemihydrate process (HH) ....
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10.4.3 Fluoride recovery and abatem
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Figure 8.1: Overview of the product
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Table 4.20: Energy balance of a dou
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ScopeSCOPEThis document on Large Vo
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Chapter 197 % of nitrogen fertilise
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Chapter 11.1.2.3 High exhaust gas v
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Chapter 1the SSD of NPK does not le
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Chapter 11,8Relative production cap
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Chapter 11.2.3 Supply of steam and
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Chapter 11.3 Overview of emissions
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Chapter 1ApplicabilityGenerally app
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Chapter 11.4.3 Handling excess stea
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Chapter 11.4.5 Optimisation/mainten
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Chapter 1Operational dataNo informa
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Chapter 1ApplicabilityEspecially ap
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Chapter 11.4.9 Environmental manage
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Chapter 1(v) Documentation- establi
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Chapter 1iv. allow for comparison w
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Chapter 1A number of studies show t
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Chapter 11.5 Common BATIn understan
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Chapter 11.5.2 BAT for environmenta
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Chapter 2Location CompanyCapacity F
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Chapter 22.2.2 Output from ammonia
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Chapter 22.2.3.2 Primary reformingT
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Chapter 2Process name Solvent/reage
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Chapter 22.2.4 Partial oxidationThe
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Chapter 2In the moving bed process,
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Chapter 22.2.6 Storage and transfer
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Chapter 2Production process Feedsto
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Chapter 22.3.2 NO x emissionsTable
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Chapter 22.3.3 Other consumption le
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Chapter 2ParameterProcessEmission l
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Chapter 22.4 Techniques to consider
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Chapter 22.4.2 Processes with reduc
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Chapter 22.4.3 Heat exchange autoth
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Chapter 22.4.4 Revamp: increase cap
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Chapter 22.4.5 Pre-reformingDescrip
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Chapter 2ApplicabilityGenerally app
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Chapter 22.4.7 Advanced process con
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Chapter 22.4.9 Combined Claus unit
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Chapter 2Operational dataSee Descri
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Chapter 22.4.12 Preheating of combu
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Chapter 22.4.14 Isothermal shift co
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Chapter 22.4.16 Stripping and recyc
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Chapter 22.4.18 Use of sulphur resi
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Chapter 22.4.20 Indirect cooling of
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Chapter 22.4.22 Ammonia removal fro
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Chapter 22.4.24 Metal recovery and
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Chapter 2Driving force for implemen
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Chapter 22.5 BAT for ammoniaBAT is
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Chapter 33 NITRIC ACID3.1 General i
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Chapter 3Pressure in bar Temperatur
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Chapter 33.2.5 Tail gas properties
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Chapter 33.3 Current emission and c
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Chapter 3N 2 O emission levelProces
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Chapter 3N 2 O emission levelProces
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Chapter 3Process typeNO x emission
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Chapter 3Process typeNO x emission
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Chapter 3140120Generation factor %1
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Chapter 33.4.2 Optimisation of the
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Chapter 33.4.3 Alternative oxidatio
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Chapter 33.4.4 Optimisation of the
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Chapter 3Achieved environmental ben
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Chapter 33.4.5 N 2 O decomposition
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Chapter 33.4.6 Catalytic N 2 O deco
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Chapter 3According to [89, Kuiper,
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Chapter 33.4.7 Combined NO x and N
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Chapter 3EconomicsInvestment costs.
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Chapter 3Operational dataSee descri
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Chapter 3NOx removal efficiency in
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Chapter 33.4.10 Addition of H 2 O 2
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Chapter 33.4.11 NO X reduction duri
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Chapter 3Installing a low temperatu
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Chapter 3NO x emission level as NO
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Chapter 3Operational dataNo specifi
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Chapter 4Country Company Location C
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Chapter 4Country Company Location C
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Chapter 4Figure 4.2 gives an overvi
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Chapter 4Two general converter type
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Chapter 4Figure 4.6 gives an impres
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Chapter 44.2.3 Sulphur sources and
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Page 192 and 193: Chapter 410Tail gas specific SO2 lo
Page 194 and 195: Chapter 4Capacity in tonnesof 100 %
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Page 198 and 199: Chapter 4SO 2 sourceSpent acid and
Page 200 and 201: Chapter 4Cross-media effectsWithout
Page 202 and 203: Chapter 4Achieved environmental ben
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
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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 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
Page 252 and 253: Chapter 5Emission of mg/l g/tonne P
Page 254 and 255: Chapter 55.4 Techniques to consider
Page 256 and 257: Chapter 55.4.2 Hemihydrate process
Page 258 and 259: Chapter 55.4.3 Hemi-dihydrate recry
Page 260 and 261: Chapter 55.4.4 Hemi-dihydrate recry
Page 262 and 263: Chapter 55.4.5 Di-hemihydrate recry
Page 264 and 265: Chapter 55.4.6 RepulpingDescription
Page 266 and 267: Chapter 55.4.7 Fluoride recovery an
Page 268 and 269: Chapter 55.4.8 Recovery and abateme
Page 270 and 271: Chapter 5Operational dataNo informa
Page 272 and 273: Chapter 55.4.11 Decadmation of H 3
Page 274 and 275: Chapter 55.4.12 Use of entrainment
Page 276 and 277: Chapter 5Cross-media effects• dis
Page 278 and 279: Chapter 5Driving force for implemen
Page 280 and 281: Chapter 5Cross-media effectsTable 5
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Page 285 and 286: Chapter 66 HYDROFLUORIC ACID6.1 Gen
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Chapter 6Component Portion (mass co
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Chapter 66.2.4 Process gas treatmen
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Chapter 6Emission of kg/tonne HF Re
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6.4 Techniques to consider in the d
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Chapter 66.4.2 Energy recovery from
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Chapter 66.4.4 Valorisation of fluo
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Chapter 66.4.6 Scrubbing of tail ga
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6.4.7 Scrubbing of tail gases: fluo
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Chapter 66.4.8 Abatement of dust em
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Chapter 66.4.9 Waste water treatmen
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Chapter 6Cross-media effects• 5 -
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Chapter 77 NPK AND CN7.1 General in
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Chapter 77.2 Applied processes and
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Chapter 77.2.3 Direct neutralisatio
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Chapter 7Fluorine compounds origina
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Chapter7Per tonne productkWh Nm 3 k
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Chapter7Emission levelmg/Nm 3 ppm k
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Chapter7Emission levelmg/Nm 3 ppm k
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7.4 Techniques to consider in the d
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Chapter7Driving force for implement
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Chapter7Achieved environmental bene
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Chapter77.4.6 Recycling warm airDes
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Chapter77.4.7 Optimising the recycl
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Chapter7Operational dataThe volume
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Chapter77.4.11 Recycling of scrubbi
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Chapter77.4.12 Waste water treatmen
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Chapter7ParameterLevelmg/Nm 3Phosph
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Chapter 88.2 Applied processes and
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Chapter 88.2.1.1 Particle formation
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Chapter 8Consumption of Per tonne u
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Chapter 8Per tonne urea Unit Remark
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Chapter 8Waste water per tonne urea
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Chapter 8Pollutant Source g/tonne u
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Chapter 8Plant Emission Amount (ton
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Chapter 8Operational dataSee Table
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Chapter 8Operational dataSee Table
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Chapter 8Driving force for implemen
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Chapter 88.4.6 Redirecting fines to
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Chapter 8Existing plantCase 2Revamp
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Chapter 88.4.8 Heat integration in
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Chapter 88.4.9 Combined condensatio
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Chapter 88.4.10 Minimisation of NH
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Chapter 8Other approaches to proces
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Chapter 88.5 BAT for Urea and UANBA
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Chapter 9Country Company LocationBe
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Chapter 99.2.2 NeutralisationThe ex
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Chapter 9Scrubbing devices• packe
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Chapter 9Pollutant mg/Nm 3 g/tonne
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Chapter 99.4 Techniques to consider
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Chapter 99.4.2 Recovery of residual
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Chapter 99.4.3 Energy consideration
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Chapter 99.4.4 Steam purification a
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Chapter 99.4.5 Autothermal granulat
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Chapter 9ApplicabilityIrrigated can
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Chapter 1010 SUPERPHOSPHATES10.1 Ge
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Chapter 10Emissionto airEmissionto
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Chapter 10Input Indirect granulatio
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Chapter 10Volume5 - 10 m 3 /hourTem
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Chapter 1010.4.2 Recovery and abate
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Chapter 1010.4.4 Recycling of scrub
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Chapter 1111 CONCLUDING REMARKS11.1
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Chapter 11Production of HNO 3 : De-
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References26 Dipankar Das (1998).
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References89 Kuiper (2001). "High t
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References147 Uhde (2006). "The Uhd
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GlossaryCalculation of steam proper
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GlossaryIPCCIPPCISO 14001Intergover
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GlossaryChemical formulasAl 2 O 3Ca
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Annexes14 ANNEXES14.1 Cost calculat
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