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Chapter 2ParameterProcessEmission levelmg/Nm 3 kg/t NH 3 ppmvRemarkReferenceMethanol Partial oxidation, CO 2 removal 600SO 2 Partial oxidation, thermal post combustion 4500 1.676CO Partial oxidation, thermal post combustion 100 0.034BOD Partial oxidation, process condensate 80 mg/l, inlet of the treatment plantParticulates 10Yara, Brunsbüttel[28, Comments on D2, 2004][3, European Commission, 1997]Methanol Partial oxidation, superheater140H 2 S0.5CO 7 0.016Methanol Partial oxidation, superheater94 0.210H 2 S0.3 0.001CO 8 0.016ParticulatesPartial oxidation, auxiliary boiler4.3 0.008Hydrocarbons 9 0.017Low NO x burnersSO 21060 1.98SO 2 Partial oxidation, Claus unit 2 % of the S-content in fuelSO 2 1340 2.18COPartial oxidation, thermal oxidiser after Claus unit5 0.001Particulates 4 0.008Hydrocarbons9 0.001NH 3 Partial oxidation, emission to water 0.130Particulates Primary reformer 556 Large Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers
Chapter 2ParameterProcessEmission levelmg/Nm 3 kg/t NH 3 ppmvRemarkReferenceAmmonia synthesis, after purge gas washer 75 0.040Fugitive emissionsAdvanced conventional process, emission to water 0.0281 tonne NH 3 /yearStripping of process condensatesand recycling to boiler feed-waterReduced primary reforming, emission to waterHeat exchange autothermal reforming, emission towaterNH 30.0320.080NegligibleSupplying process steam by feedgas saturation with processcondensates[3, European Commission, 1997]Emissions to water before installation of astripping unit0.7 25 m 3 /hour0.8 49 m 3 /hourNH 3 slip from SNCR at primary reformer 1.1 – 5.1 Measured 4 times/year[9, Austrian UBA, 2002]Purge gas from ammonia synthesis18 kg NH 3 /year0.0140.011Ammonia synthesis, emissions to air[6, German UBA, 2000]CO 0.006Hydrocarbons0.0090.2 Catalysts and molecular sieves [3, European Commission, 1997]WasteIn general0.07 Spent catalysts, 13 tonnes/year0.09 Spent catalysts, 31 tonnes/year[9, Austrian UBA, 2002]Table 2.9: Other emission levels reported for the production of ammoniaLarge Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers 57
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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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Page 36 and 37: Chapter 11,8Relative production cap
Page 38 and 39: Chapter 11.2.3 Supply of steam and
Page 40 and 41: Chapter 11.3 Overview of emissions
Page 42 and 43: Chapter 1ApplicabilityGenerally app
Page 44 and 45: Chapter 11.4.3 Handling excess stea
Page 46 and 47: Chapter 11.4.5 Optimisation/mainten
Page 48 and 49: Chapter 1Operational dataNo informa
Page 50 and 51: Chapter 1ApplicabilityEspecially ap
Page 52 and 53: Chapter 11.4.9 Environmental manage
Page 54 and 55: Chapter 1(v) Documentation- establi
Page 56 and 57: Chapter 1iv. allow for comparison w
Page 58 and 59: Chapter 1A number of studies show t
Page 60 and 61: Chapter 11.5 Common BATIn understan
Page 62 and 63: Chapter 11.5.2 BAT for environmenta
Page 64 and 65: Chapter 2Location CompanyCapacity F
Page 66 and 67: Chapter 22.2.2 Output from ammonia
Page 68 and 69: Chapter 22.2.3.2 Primary reformingT
Page 70 and 71: Chapter 2Process name Solvent/reage
Page 72 and 73: Chapter 22.2.4 Partial oxidationThe
Page 74 and 75: Chapter 2In the moving bed process,
Page 76 and 77: Chapter 22.2.6 Storage and transfer
Page 78 and 79: Chapter 2Production process Feedsto
Page 80 and 81: Chapter 22.3.2 NO x emissionsTable
Page 82 and 83: Chapter 22.3.3 Other consumption le
Page 86 and 87: Chapter 22.4 Techniques to consider
Page 88 and 89: Chapter 22.4.2 Processes with reduc
Page 90 and 91: Chapter 22.4.3 Heat exchange autoth
Page 92 and 93: Chapter 22.4.4 Revamp: increase cap
Page 94 and 95: Chapter 22.4.5 Pre-reformingDescrip
Page 96 and 97: Chapter 2ApplicabilityGenerally app
Page 98 and 99: Chapter 22.4.7 Advanced process con
Page 100 and 101: Chapter 22.4.9 Combined Claus unit
Page 102 and 103: Chapter 2Operational dataSee Descri
Page 104 and 105: Chapter 22.4.12 Preheating of combu
Page 106 and 107: Chapter 22.4.14 Isothermal shift co
Page 108 and 109: Chapter 22.4.16 Stripping and recyc
Page 110 and 111: Chapter 22.4.18 Use of sulphur resi
Page 112 and 113: Chapter 22.4.20 Indirect cooling of
Page 114 and 115: Chapter 22.4.22 Ammonia removal fro
Page 116 and 117: Chapter 22.4.24 Metal recovery and
Page 118 and 119: Chapter 2Driving force for implemen
Page 120 and 121: Chapter 22.5 BAT for ammoniaBAT is
Page 123 and 124: Chapter 33 NITRIC ACID3.1 General i
Page 125 and 126: Chapter 3Pressure in bar Temperatur
Page 127 and 128: Chapter 33.2.5 Tail gas properties
Page 129 and 130: Chapter 33.3 Current emission and c
Page 131 and 132: Chapter 3N 2 O emission levelProces
Page 133 and 134: 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 44.3 Current emission and c
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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 4Driving force for implemen
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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 Techniques to consider
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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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Chapter 55.4.11 Decadmation of H 3
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Chapter 55.4.12 Use of entrainment
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Chapter 5Cross-media effects• dis
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Chapter 5Cross-media effectsTable 5
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Chapter 5ApplicabilityAt present, o
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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 77.2.3 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 88.2.1.1 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 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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