integration of solid oxide fuel cells and ... - Ea Energianalyse

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3. COMPONENT DESCRIPTION surroundings). Ḣ r,i + Ḣ c,i = Ḣ r,o + Ḣ c,o + ˙Q loss (3.24) The mass balance is specified for the refrigerant as well as the coolant. ṁ r,o = ṁ r,i (3.25) ṁ c,o = ṁ c,i (3.26) The pressure losses (given as a negative pressure increases) are defined as two different ∆p parameters: p r,o = p r,i + ∆p r (3.27) p c,o = p c,i + ∆p c (3.28) 52
3.6. Desorber - DES 3.6 Desorber - DES In the desorber the weak water-LiBr solution enters (either sub cooled or saturated liquid) and is mixed with the solution in the desorber, which is heated up by the heating water circuit. Hereby the refrigerant (water) is evaporated, and strong solution LiBr (which is saturated) is returned towards the absorber. See figure 3.7. Figure 3.7: Desorber component. Weak solution (ws,i) enters the desorber and is heated by the heating water (h,i and h,o). Refrigerant in gas phase (r,o) is sent out through an outlet at the top, while the strong solution (ss,o) leaves at the bottom of the desorber. The desorber is made up by a reservoir of solution in which some heat exchanger tubes with the warm heating water run. On top there is a gas phase of refrigerant. In the model it is assumed that the temperature is the same throughout the liquid phase and the gas phase. So when the weak LiBr solution enters the reservoir, it instantly becomes perfectly mixed with the rest of the liquid phase. It is also assumed that the outlet temperature of the refrigerant (superheated steam) is the same as the outlet temperature of the solution, after all, the water has been evaporated from the solution (at which point they must have the same temperature), and no heating or cooling is assumed to happen to the gas after the evaporation (hence T ss,o = T r,o ), see figure 3.8. Since it is assumed that the temperature of the solution is the same throughout the desorber, only the heating water changes temperature. Hence the closest approach temperature difference appears between the outlet temperature of the heating water (T h,o ) and the mutual temperature of the refrigerant and solution (T ss,o = T r,o ): ∆T minr,o = T h,o − T ss,o (3.29) Since only the heating water changes temperature during the heat exchange process, the effectiveness will be based on the heating water 53
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INTEGRATION OF SOLID OXIDE FUEL CEL
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Abstract It is investigated whether
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Preface This report is documentatio
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CONTENTS Preface . . . . . . . . .
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CONTENTS 4.2.3 SOFC stack . . . . .
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CONTENTS A.4 DG appendix . . . . .
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LIST OF FIGURES 4.3 Diagram of sing
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NOMENCLATURE Acronyms Acronym ABS A
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Greek (and other) Symbols Greek (an
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Subscripts Subscripts Subscript 2P
Page 28 and 29: 1. INTRODUCTION Chapter 4, System d
Page 30 and 31: 1. INTRODUCTION the electricity and
Page 32 and 33: 1. INTRODUCTION 1.4 SOFC The fuel c
Page 34 and 35: 1. INTRODUCTION 1.5 Heat driven coo
Page 36 and 37: 1. INTRODUCTION Cycle description.
Page 38 and 39: 1. INTRODUCTION Ammonia-water The C
Page 40 and 41: 1. INTRODUCTION 1.5.3 Platen Munter
Page 42 and 43: 1. INTRODUCTION Open loop In an ope
Page 44 and 45: 1. INTRODUCTION 1.7 Problem stateme
Page 46 and 47: 2. MARKET INVESTIGATION appendix A.
Page 48 and 49: 2. MARKET INVESTIGATION 2.2.2 Ship
Page 50 and 51: 2. MARKET INVESTIGATION Pay Back Ti
Page 52 and 53: 2. MARKET INVESTIGATION 2.3.2 Micro
Page 54 and 55: 2. MARKET INVESTIGATION Sensitivity
Page 56 and 57: 2. MARKET INVESTIGATION • ECH pri
Page 58 and 59: 2. MARKET INVESTIGATION 2.4.3 Resul
Page 60 and 61: 2. MARKET INVESTIGATION 16000 14000
Page 62 and 63: 2. MARKET INVESTIGATION Annuity pri
Page 64 and 65: 2. MARKET INVESTIGATION 2.4.4 Concl
Page 67 and 68: C H A P T E R 3 COMPONENT DESCRIPTI
Page 69 and 70: 3.1. Introduction The seven stream
Page 71 and 72: 3.2. Absorber - ABSO 3.2 Absorber -
Page 73 and 74: 3.2. Absorber - ABSO implicitly thr
Page 75 and 76: 3.4. Burner - BURN 3.4 Burner - BUR
Page 77: 3.5. Condenser - COND T [° C ] ΔT
Page 81 and 82: 3.7. Evaporator - EVAP 3.7 Evaporat
Page 83 and 84: 3.8. Heat Exchanger - HEX 3.8 Heat
Page 85 and 86: 3.8. Heat Exchanger - HEX The press
Page 87 and 88: 3.10. Pre Reformer - PR 3.10 Pre Re
Page 89 and 90: 3.11. Pump - PUMP 3.11 Pump - PUMP
Page 91 and 92: 3.12. Solid Oxide Fuel Cell - SOFC
Page 97 and 98: 3.14 Cooling Tower - TOWER 3.14. Co
Page 99 and 100: 3.14. Cooling Tower - TOWER tower d
Page 101 and 102: 3.14. Cooling Tower - TOWER The air
Page 103: 3.15. Expansion valve - VA/VB possi
Page 106 and 107: 4. SYSTEM DESCRIPTION 8 SPG 10 20 1
Page 108 and 109: 4. SYSTEM DESCRIPTION Pre reformer
Page 110 and 111: 4. SYSTEM DESCRIPTION which increas
Page 112 and 113: 4. SYSTEM DESCRIPTION 4.3 Absorptio
Page 114 and 115: 4. SYSTEM DESCRIPTION 4.3.3 Pumping
Page 116 and 117: 4. SYSTEM DESCRIPTION The temperatu
Page 118 and 119: 4. SYSTEM DESCRIPTION 4.5 Absorptio
Page 120 and 121: 4. SYSTEM DESCRIPTION 4.6 Cooling T
Page 122 and 123: 4. SYSTEM DESCRIPTION (below 100
Page 124 and 125: 4. SYSTEM DESCRIPTION as: Ẇ AC =
Page 126 and 127: 4. SYSTEM DESCRIPTION 4.8 Verificat
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4. SYSTEM DESCRIPTION SOFC net effi
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C H A P T E R 5 SIMULATION AND RESU
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5.1. Basic absorption cooling Figur
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5.1. Basic absorption cooling geous
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5.1.3 Changing evaporator temperatu
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5.1. Basic absorption cooling as de
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5.2. System configurations Red repr
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5.2. System configurations Dual Hea
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5.2. System configurations in a hot
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5.3. Partial optimization of standa
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Anode recycling (α SPG1 ) 5.3. Par
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Page 167 and 168:
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5.4. Sensitivity Analysis ηsys,el,
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5.4. Sensitivity Analysis the press
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5.4. Sensitivity Analysis 1. The x-
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5.5 Total optimization of system 5.
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5.5. Total optimization of system i
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5.5. Total optimization of system e
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C H A P T E R 6 CASES AND ECONOMICS
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6.2. High humidity climate BBC Home
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6.2. High humidity climate Figure 6
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6.3. Low humidity climate Figure 6.
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6.4. Economics 6.4 Economics When t
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C H A P T E R 7 DISCUSSION In this
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7.1.1 Accuracy and sensitivity 7.1.
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7.2. Economical considerations Furt
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7.2.3 Distributed Generation (DG) D
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7.2. Economical considerations to 6
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7.2. Economical considerations As m
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C H A P T E R 8 CONCLUSION System c
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For the APU segment a SOFC-ABS syst
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C H A P T E R 9 FURTHER WORK Some i
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BIBLIOGRAPHY [1] Acfshop.dk: http:/
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Bibliography [24] Nordea invest: ht
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Appendices 187
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A. MARKET INVESTIGATION A.1 Market
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A. MARKET INVESTIGATION No cost for
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Absorpton unit (free waste heat) Pr
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A. MARKET INVESTIGATION A.3 CHP app
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Absorption Refrigerator RGE 400 fro
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Sensitivity analysis The effect on
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A. MARKET INVESTIGATION A.4 DG appe
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From the "CHP in the Hotel and Casi
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Hotel with 230 rooms and 18000 m^2
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SOFC + Water Heating (no ABS), Cool
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16000 Pay Back Time: Entire System
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SOFC + Water Heating (no ABS), Cool
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Hot climate SOFC + ABS + HW vs pure
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Assumptions SOFC price = 2650kr/kW
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Hot climate Increase (Delta NPV_10)
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Prices of absorption cooling units
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1'000'000 900'000 800'000 143'600 7
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A. MARKET INVESTIGATION A.6 Gas and
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Retail electricity prices Exchange
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B. DIAGRAMS AND PLOTS B.1 GAX diagr
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B. DIAGRAMS AND PLOTS B.3 Closed ad
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B. DIAGRAMS AND PLOTS B.4.2 p-T dia
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C. EES Efficiencies SOFC η inver t
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C. EES ∆ p;GGHE X 1;c = −1 [kPa
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C. EES ˙Q loss;Bur n = 0 [kW ] ˙Q
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C. EES SOFC ∆ T ;SOFC ;av = 30 [C
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C. EES C.2 Results - Standard param
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C. EES 244 DES2 h;o = 42 DES2 i = 7
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C. EES SOFC ano;i = 5 SOFC ano;o =
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C. EES Point T i p i ṁ i qu i h i
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C. EES C.3 Results - Optimized para
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C. EES ∆ T ;min;W GHE X 3;w;i = 1
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C. EES ˙Q tr ans;W GHE X 3 = 2,752
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C. EES Point T i p i ṁ i qu i h i
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C. EES C.4 Results - Uncertainty pr
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C. EES ∆T ;min;W GHE X 3;w;i = 15
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C. EES ∆p;TOW ER1;air ;dr y = 0,1
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C. EES ∆p;GGHE X 1;c = −1 ±
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C. EES C.4.4 ∆p for absorption su
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C. EES C.4.5 ˙Qloss for absorption
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A P P E N D I X D OTHER D.1 Explana
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D.3. Water consumption Hence it is
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A P P E N D I X E OPTIMIZATION GRAP
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E.1. Simulations and Results E.1.2
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E.1. Simulations and Results Figure
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E.1. Simulations and Results Figure
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E.2. Cases E.2 Cases E.2.1 Extreme
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SEG Scandinavian Energy Group Aps.
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8 SPG 1 10 1-α GGHEX1 9 α 7 GGHEX
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1 8 GGHEX1 CH4, in Air, in 21 2 11
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