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

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4. SYSTEM DESCRIPTION The temperature difference between point 41 and point 42 (∆T h,DES2 ) is 5 ◦ C like for DES1. The temperature of DES2 is 150 ◦ C (point 70 and 79). The high pressure refrigerant is sent to COND2 inlet (point 71). Like for COND1 in the single stage cycle configuration, the refrigerant is both de-superheated and condensed in COND2. Thus the closest approach temperature difference is found somewhere between point 71 and point 72. Due to limitations in the model it is not possible to set this parameter directly and instead ∆T min,COND2,r,o is set to 12,5 ◦ C. This corresponds to ∆T min,COND2,mp being 10 ◦ C. The heat from COND2 is removed by the heat transferring loop (point 31 to point 34) and supplied to low temperature desorber DES1. The loop is modeled as a water circuit, but in a real double stage unit, COND2 and DES1 would be integrated as one component. The saturated liquid refrigerant (qu 72 = 0) is expanded in VA2 point 72 before it is mixed with superheated refrigerant from DES1 point 50 in MIXR1. The quality of the refrigerant outlet is between zero and one in point 51. Unlike COND2, the refrigerant entering COND1 is not superheated. Thus the closest approach temperature difference exists at the inlet in point 51 (compared to the temperature in point 36) but the value is still 10 ◦ C. The heat from COND2 is removed by the cooling circuit (point 35 and point 36) The refrigerant is expanded in VA1 (point 53), then evaporated (point 54), and absorbed in the absorber exactly the same way as in the single stage cycle. The difference occurs after the weak solution is preheated in SHEX1 in point 57. In the double stage system only some of the solution is sent to DES1 but the remaining part is pressurized further by PUMP2 (point 76) and preheated in SHEX2 (point 77) before it enters DES2 (point 78). The strong solution is cooled in SHEX2 (point 80 to 81), expanded in VB2 and mixed with the strong solution coming from DES1 in MIXL1. Since the temperature in point 50 is not set as a parameter (as it is the case for the single stage cycle), another relation is given: ṁ 70 ṁ 78 = ṁ50 ṁ 58 (4.4) This relation determines the fraction of solution which is sent to the DES2. It also implies that concentration of the weak and strong solution will be the same for the two solutions in the two circuits (w 55 = w 75 90
4.4. Absorption Double Stage and w 59 = w 79 ). This has been done for two reasons. First of all it gives a value of T 50 = 78 ◦ C which is quite close to optimum. Secondly if other parameters like the temperature of the high pressure desorber is increased then T 50 will increase as well and thereby remain near optimum for the given T 70 . 91
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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
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1. INTRODUCTION Chapter 4, System d
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1. INTRODUCTION the electricity and
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1. INTRODUCTION 1.4 SOFC The fuel c
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1. INTRODUCTION 1.5 Heat driven coo
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1. INTRODUCTION Cycle description.
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1. INTRODUCTION Ammonia-water The C
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1. INTRODUCTION 1.5.3 Platen Munter
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1. INTRODUCTION Open loop In an ope
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1. INTRODUCTION 1.7 Problem stateme
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2. MARKET INVESTIGATION appendix A.
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2. MARKET INVESTIGATION 2.2.2 Ship
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2. MARKET INVESTIGATION Pay Back Ti
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2. MARKET INVESTIGATION 2.3.2 Micro
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2. MARKET INVESTIGATION Sensitivity
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2. MARKET INVESTIGATION • ECH pri
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2. MARKET INVESTIGATION 2.4.3 Resul
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2. MARKET INVESTIGATION 16000 14000
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2. MARKET INVESTIGATION Annuity pri
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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 and 78: 3.5. Condenser - COND T [° C ] ΔT
Page 79 and 80: 3.6. Desorber - DES 3.6 Desorber -
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 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
Page 128 and 129: 4. SYSTEM DESCRIPTION SOFC net effi
Page 131 and 132: C H A P T E R 5 SIMULATION AND RESU
Page 133 and 134: 5.1. Basic absorption cooling Figur
Page 135 and 136: 5.1. Basic absorption cooling geous
Page 137 and 138: 5.1.3 Changing evaporator temperatu
Page 139 and 140: 5.1. Basic absorption cooling as de
Page 141 and 142: 5.2. System configurations Red repr
Page 143 and 144: 5.2. System configurations Dual Hea
Page 145 and 146: 5.2. System configurations in a hot
Page 147 and 148: 5.3. Partial optimization of standa
Page 155 and 156: Anode recycling (α SPG1 ) 5.3. Par
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5.3. Partial optimization of standa
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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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