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Chapter 7Emission levelmg/Nm 3 ppm kg/hourRemarkReference60 Nitrophosphate route, including conversion units [76, EFMA, 2000]6 0.05 – 0.07 8000 – 12000 m 3 /hour, exhaust gases from wet process part (phosphate rock digestion), wet scrubbers Compo, Krefeld1 – 3 0.02 – 0.06 19000 m 3 /hour, exhaust gas from digestion of Florida phosphate rock, wet scrubber BASF, Ludwigshafen1 – 2.7 0.34 – 0.92340000 m 3 /hour, exhaust gases from neutralisation, granulation, drying, conditioning , cyclones andscrubberBASF, LudwigshafenFluoride as HF3.2 0.511.65 0.4160000 m 3 /hour, exhaust gas from granulation/pipe reactor, drying, cooling and screening, cyclones and3-stage scrubbing250000 m 3 /hour, combined scrubbing of exhaust gas from neutralisation/evaporation and granulation(see Section 7.4.10)DonauchemieAMI, Linz0.34 0.008 25000 m 3 /hour, levels from 2001, digestion of phosphate rock, multistage scrubbing (see Section 7.4.9) AMI, Linz0.30 0.008 25000 m 3 /hour, levels from 2000, digestion of phosphate rock, multistage scrubbing (see Section 7.4.9) AMI, Linz1.4 – 2.0 Mixed acid route, pipe reactor, 3-stage scrubbingCFL, India[79, Carillo, 2002]5 6 Mixed acid route, indicative levels [77, EFMA, 2000]5 Nitrophosphate route and conversion units [76, EFMA, 2000]Dust40 – 75 3.6 – 6.8 90000 m 3 /hour, exhaust gases from dry process part, cyclones only Compo, Krefeld16.8 Drum granulator, drying drum, cyclones and scrubber AMFERT, Amsterdam10 – 35 3.4 – 11.926.6 6.770 11.2340000 m 3 /hour, exhaust gases from neutralisation, granulation, drying, conditioning , cyclones andscrubber250000 m 3 /hour, combined scrubbing of exhaust gas from neutralisation/evaporation and granulation(see Section 7.4.10)160000 m 3 /hour, exhaust gas from granulation/pipe reactor, drying, cooling and screening, cyclones and3-stage scrubbingBASF, LudwigshafenAMI, LinzDonauchemie294 Large Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers
Chapter7Emission levelmg/Nm 3 ppm kg/hourRemarkReference30 – 40 Mixed acid route, pipe reactor, 3-stage scrubbingCFL, India[79, Carillo, 2002]5 2.5 500000 m 3 /hour, nitrophosphate route, emission from prill tower, no abatement20 7.4 370000 m 3 /hour, CN production, emission from prill tower, no abatement[76, EFMA, 2000]50 Wet dust expressed as dry matter, mixed acid route23 3.7160000 m 3 /hour, exhaust gas from granulation/pipe reactor, drying, cooling and screening, cyclones and3-stage scrubbingDonauchemie3.7 Exhaust gas from drying drum, cyclones and scrubber AMFERTHCl15 Exhaust gas from drum granulator and drying
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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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Chapter 44.2.3.5 Non-ferrous metal
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Chapter 4Sulphur source/SO 2 produc
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Chapter 410Tail gas specific SO2 lo
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Chapter 4Capacity in tonnesof 100 %
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Chapter 4Capacity in tonnesof 100 %
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Chapter 4SO 2 sourceSpent acid and
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Chapter 4Cross-media effectsWithout
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Chapter 44.4.3 Addition of a 5 th b
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Chapter 44.4.4 Application of a Cs-
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Chapter 4EUR/yearWaste gas volume (
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Chapter 44.4.6 Replacement of brick
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Chapter 4EUR/yearWaste gas volume (
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Chapter 4PlantSO 2 sourceInlet SO 2
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Chapter 44.4.10 Combination of SCR
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Chapter 44.4.14 Monitoring of SO 2
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Chapter 4EconomicsCost benefits can
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Chapter 4Energy inputRecovery and l
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Chapter 44.4.16 Minimisation and ab
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Chapter 44.4.17 Minimisation of NO
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Chapter 44.4.19 Tail gas scrubbing
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Chapter 44.4.21 Tail gas treatment:
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Chapter 4Economics[58, TAK-S, 2003]
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Chapter 4EconomicsNo specific infor
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Chapter 4BAT is to minimise and red
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Chapter 55.2 Applied processes and
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Chapter 55.2.2.1 Raw materials5.2.2
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Chapter 5OriginChinaMine/regionRare
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Chapter 55.2.2.2 GrindingDepending
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Chapter 5Emission of mg/l g/tonne P
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Chapter 55.4.2 Hemihydrate process
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Chapter 55.4.3 Hemi-dihydrate recry
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Chapter 55.4.4 Hemi-dihydrate recry
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Chapter 55.4.5 Di-hemihydrate recry
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Chapter 55.4.6 RepulpingDescription
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Chapter 55.4.7 Fluoride recovery an
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Chapter 55.4.8 Recovery and abateme
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Chapter 5Operational dataNo informa
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Page 274 and 275: Chapter 55.4.12 Use of entrainment
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Page 278 and 279: Chapter 5Driving force for implemen
Page 280 and 281: Chapter 5Cross-media effectsTable 5
Page 282 and 283: Chapter 5ApplicabilityAt present, o
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Page 289 and 290: Chapter 66.2.4 Process gas treatmen
Page 291 and 292: Chapter 66.3 Current emission and c
Page 293 and 294: Chapter 6Emission of kg/tonne HF Re
Page 295 and 296: 6.4 Techniques to consider in the d
Page 297 and 298: Chapter 66.4.2 Energy recovery from
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Page 301 and 302: Chapter 66.4.6 Scrubbing of tail ga
Page 303 and 304: 6.4.7 Scrubbing of tail gases: fluo
Page 305 and 306: Chapter 66.4.8 Abatement of dust em
Page 307 and 308: Chapter 66.4.9 Waste water treatmen
Page 309 and 310: Chapter 6Cross-media effects• 5 -
Page 311 and 312: Chapter 77 NPK AND CN7.1 General in
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Page 315 and 316: Chapter 77.2.3 Direct neutralisatio
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Page 319 and 320: Chapter7Per tonne productkWh Nm 3 k
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Page 337 and 338: Chapter77.4.7 Optimising the recycl
Page 339 and 340: Chapter7Operational dataThe volume
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Page 354 and 355: Chapter 88.2.1.1 Particle formation
Page 356 and 357: Chapter 8Consumption of Per tonne u
Page 358 and 359: Chapter 8Per tonne urea Unit Remark
Page 360 and 361: Chapter 8Waste water per tonne urea
Page 362 and 363: Chapter 8Pollutant Source g/tonne u
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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 99.4.2 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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