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 2Driving force for implementationEmission reduction.References to literature and example plants[3, European Commission, 1997]90 Large Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers
2.4.26 Ammonia production using hydrogen from water electrolysisDescriptionChapter 2Electrolytically produced hydrogen can be used directly for the production of ammonia, andsuch operations existed in the mid 1990s in Egypt, Iceland and Peru. In this process, hydrogenfrom the water electrolysis plant and nitrogen from the air separation plant pass to separatestorage vessels, providing a buffer capacity and a stabilised gas pressure. Water electrolysisgives an extremely pure feed gas, containing only a very small amount of oxygen (0.1 – 0.2 %),compared to the synthesis gas generated from a hydrocarbon feedstock. Oxygen acts as a poisonto the ammonia converter catalyst and has therefore to be removed. This is carried out by meansof catalytic combustion, which takes place immediately after the mixing of hydrogen andnitrogen. A small amount of hydrogen reacts with the oxygen present producing water. Thepurified mixed gas (make-up gas) is then passed to a storage vessel that serves as a buffer forthe ammonia synthesis stage. The synthesis loop is the same as for fossil fuel-based ammoniaplants.Achieved environmental benefitsDirect emissions from this process are minimal compared to the steam reforming and partialoxidation process.Cross-media effectsNone believed likely.Operational dataNo specific information provided.ApplicabilityAmmonia production based on water electrolysis is currently carried out in plants of up to500 tonnes/day. The process is generally not considered economically viable. However, undercertain local circumstances (depending on the local price for electric power), it can still be aninteresting and competitive technology, in particular when renewable electric power isabundantly available.EconomicsThe process is generally not considered economically viable due to the actual price for electricpower.Driving force for implementationLocal considerations.References to literature and example plants[1, EFMA, 2000, 3, European Commission, 1997]Large Volume Inorganic Chemicals – Ammonia, Acids and Fertilisers 91
- 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 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
Chapter 2Driving force for implementationEmission reduction.References to literature and example plants[3, European Commission, 1997]90 <strong>Large</strong> <strong>Volume</strong> <strong>Inorganic</strong> <strong>Chemicals</strong> – <strong>Ammonia</strong>, Acids and Fertilisers