Large Volume Inorganic Chemicals - Ammonia ... - ammk-rks.net

More documents

Recommendations

Info

Chapter 55.4.2 Hemihydrate process (HH)DescriptionThe process operating conditions are set to enable calcium sulphate to be precipitated as thehemihydrate. In this way it is possible to produce 40 – 46 % P 2 O 5 acid directly, enablingvaluable savings to be made in energy usage. Figure 5.4 gives an overview of the hemihydrateprocess.Acid from the hemihydrate process tends to contain much less free sulphate and suspendedsolids and lower levels of aluminium and fluorine than evaporated dihydrate process acids ofthe same strength. Additionally, a satisfactory rate of reaction can be achieved from muchcoarser rock than in the dihydrate process, because of the more severe reaction conditions in thehemihydrate process.CondenserVacuumWaste gasPhosphate rockVenturiscrubberFlashcoolerH 2OAttack tanksAgingtankH 2SO 4H 2OGypsumHemihydrate CaSO . 4½H 2OfiltrationH 3PO 4Weak acid40 – 46 % P 2O 5Figure 5.4: Overview of the hemihydrate process[31, EFMA, 2000]Hemihydrate crystals tend to be small and less well formed than dihydrate crystals sohemihydrate slurries tend to be more difficult to filter than dihydrate slurries, unless crystalform modifiers are used to suppress excessive nucleation. With a good hemihydrate processhowever, there is no need to use modifiers.The amount of wash-water that can be used is restricted by water balance needs. Additionally asa result of the higher P 2 O 5 concentration of the slurry being filtered, the amounts of both solubleand insoluble P 2 O 5 remaining in the filter cake are greater. However, despite these losses thesimplicity of the hemihydrate plant and the absence of silicofluoride and chukhrovite (acrystallised mineral compound) scaling in the hemihydrate filter may compensate for the higherinsoluble P 2 O 5 losses through the hemihydrate cake.Hemihydrate is not a stable form of calcium sulphate so there is a tendency for it to revert togypsum even before the acid has been filtered off. The conditions are even more favourable forrehydration during washing. In a well run hemihydrate plant, there is no conversion in thereactor train. A small quantity of anti-scaling agent may be required in a single-stagehemihydrate plant filter to minimise scaling.228 Large Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers
Chapter 5The cake is more acidic than gypsum filter cake because of the extra P 2 O 5 losses. It alsocontains more fluoride and cadmium.The demands on vulnerable items of equipment, particularly agitators and slurry pumps, areincreased as a result of the higher temperature (100 ºC) and acidic concentration (40 – 50 %P 2 O 5 ) in comparison to a dihydrate plant.Achieved environmental benefits• energy savings due to reduction or elimination of the need for evaporation• energy savings due to lower rock grinding requirements (may use coarse rock).Cross-media effects• low P 2 O 5 efficiency: 90 – 94 %• produces impure hemihydrate (1.1 % P 2 O 5 ).Operational dataSee description.ApplicabilityGenerally applicable. Limited number of rocks processed industrially. The overall efficiencydepends on the rock type.EconomicsRequires higher grade alloys in comparison to processes with lower temperature.Driving force for implementationCost benefits.References to literature and example plants[29, RIZA, 2000, 31, EFMA, 2000], Kemira Chemicals Oy, FinlandLarge Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers 229
Page 1 and 2:
EUROPEAN COMMISSIONIntegrated Pollu
Page 3 and 4:
Executive SummaryEXECUTIVE SUMMARYT
Page 5 and 6:
Executive SummaryII.Production and
Page 7 and 8:
Executive Summarybed, using a cesiu
Page 9 and 10:
Executive SummaryConversion process
Page 11 and 12:
Executive SummaryBAT is to treat al
Page 13 and 14:
PrefacePREFACE1. Status of this doc
Page 15 and 16:
Preface5. How to understand and use
Page 17 and 18:
2.2.4.2 Gasification of heavy hydro
Page 19 and 20:
5.4.2 Hemihydrate process (HH) ....
Page 21 and 22:
10.4.3 Fluoride recovery and abatem
Page 23 and 24:
Figure 8.1: Overview of the product
Page 25 and 26:
Table 4.20: Energy balance of a dou
Page 27:
ScopeSCOPEThis document on Large Vo
Page 30 and 31:
Chapter 197 % of nitrogen fertilise
Page 32 and 33:
Chapter 11.1.2.3 High exhaust gas v
Page 34 and 35:
Chapter 1the SSD of NPK does not le
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 84 and 85:
Chapter 2ParameterProcessEmission l
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
Page 135 and 136:
Chapter 3Process typeNO x emission
Page 137 and 138:
Chapter 3Process typeNO x emission
Page 139 and 140:
Chapter 3140120Generation factor %1
Page 141 and 142:
Chapter 33.4.2 Optimisation of the
Page 143 and 144:
Chapter 33.4.3 Alternative oxidatio
Page 145 and 146:
Chapter 33.4.4 Optimisation of the
Page 147 and 148:
Chapter 3Achieved environmental ben
Page 149 and 150:
Chapter 33.4.5 N 2 O decomposition
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:
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 202 and 203:
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
Page 252 and 253: Chapter 5Emission of mg/l g/tonne P
Page 254 and 255: Chapter 55.4 Techniques to consider
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
Page 282 and 283: Chapter 5ApplicabilityAt present, o
Page 285 and 286: Chapter 66 HYDROFLUORIC ACID6.1 Gen
Page 287 and 288: Chapter 6Component Portion (mass co
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
Page 299 and 300: Chapter 66.4.4 Valorisation of fluo
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
Page 313 and 314:
Chapter 77.2 Applied processes and
Page 315 and 316:
Chapter 77.2.3 Direct neutralisatio
Page 317 and 318:
Chapter 7Fluorine compounds origina
Page 319 and 320:
Chapter7Per tonne productkWh Nm 3 k
Page 321 and 322:
Chapter7Emission levelmg/Nm 3 ppm k
Page 323 and 324:
Chapter7Emission levelmg/Nm 3 ppm k
Page 325 and 326:
7.4 Techniques to consider in the d
Page 327 and 328:
Chapter7Driving force for implement
Page 329 and 330:
Page 331 and 332:
Page 333 and 334:
Chapter7Achieved environmental bene
Page 335 and 336:
Chapter77.4.6 Recycling warm airDes
Page 337 and 338:
Chapter77.4.7 Optimising the recycl
Page 339 and 340:
Chapter7Operational dataThe volume
Page 341 and 342:
Page 343 and 344:
Page 345 and 346:
Chapter77.4.11 Recycling of scrubbi
Page 347 and 348:
Chapter77.4.12 Waste water treatmen
Page 349:
Chapter7ParameterLevelmg/Nm 3Phosph
Page 352 and 353:
Chapter 88.2 Applied processes and
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
Page 364 and 365:
Chapter 8Plant Emission Amount (ton
Page 366 and 367:
Page 368 and 369:
Chapter 8Operational dataSee Table
Page 370 and 371:
Chapter 8Operational dataSee Table
Page 372 and 373:
Chapter 8Driving force for implemen
Page 374 and 375:
Chapter 88.4.6 Redirecting fines to
Page 376 and 377:
Chapter 8Existing plantCase 2Revamp
Page 378 and 379:
Chapter 88.4.8 Heat integration in
Page 380 and 381:
Chapter 88.4.9 Combined condensatio
Page 382 and 383:
Chapter 88.4.10 Minimisation of NH
Page 384 and 385:
Page 386 and 387:
Chapter 8Other approaches to proces
Page 388 and 389:
Page 390 and 391:
Chapter 88.5 BAT for Urea and UANBA
Page 392 and 393:
Chapter 9Country Company LocationBe
Page 394 and 395:
Chapter 99.2.2 NeutralisationThe ex
Page 396 and 397:
Chapter 9Scrubbing devices• packe
Page 398 and 399:
Page 400 and 401:
Chapter 9Pollutant mg/Nm 3 g/tonne
Page 402 and 403:
Chapter 99.4 Techniques to consider
Page 404 and 405:
Chapter 99.4.2 Recovery of residual
Page 406 and 407:
Chapter 99.4.3 Energy consideration
Page 408 and 409:
Chapter 99.4.4 Steam purification a
Page 410 and 411:
Chapter 99.4.5 Autothermal granulat
Page 412 and 413:
Chapter 9ApplicabilityIrrigated can
Page 415 and 416:
Chapter 1010 SUPERPHOSPHATES10.1 Ge
Page 417 and 418:
Chapter 10Emissionto airEmissionto
Page 419 and 420:
Chapter 10Input Indirect granulatio
Page 421 and 422:
Chapter 10Volume5 - 10 m 3 /hourTem
Page 423 and 424:
Chapter 1010.4.2 Recovery and abate
Page 425 and 426:
Chapter 1010.4.4 Recycling of scrub
Page 427 and 428:
Chapter 1111 CONCLUDING REMARKS11.1
Page 429:
Chapter 11Production of HNO 3 : De-
Page 432 and 433:
References26 Dipankar Das (1998).
Page 434 and 435:
References89 Kuiper (2001). "High t
Page 436 and 437:
References147 Uhde (2006). "The Uhd
Page 438 and 439:
GlossaryCalculation of steam proper
Page 440 and 441:
GlossaryIPCCIPPCISO 14001Intergover
Page 442 and 443:
GlossaryChemical formulasAl 2 O 3Ca
Page 445 and 446:
Annexes14 ANNEXES14.1 Cost calculat
show all

Large Volume Inorganic Chemicals - Ammonia ... - ammk-rks.net

Create successful ePaper yourself

Delete template?

Save as template?