Design og modellering af metanolanlæg til VEnzin-visionen Bilag

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0 1 1 1 P 2 M type NOD* 1 1 type NOD* 1 1 1 Energy flow 2 Cost flow type NOD* 1 2 1 Exergy efficiency 2 Exergy destruction Water Steam 3T 2 1 3Exergy destruction cost flow - based on specific cost of input 2.4 -0 0.0 0.006 4H 3 0 4Exergy destruction cost flow - based on specific cost of output 1 1.0 bar Electrolyser 423 10.0 bar 0.02 412 2 5EX 6 EX_CH * Number of decimals 5 Component cost flow Electrolyser 2 0.076 2.4 kg/s 15 C 39.7 MW SAND 201 39.71 2 0.00 0.0 kg/s 850 C 0.0 0.176 10.0 bar 0.0 kg/s NG 7 EX_PH SAND 301 Electrolyser NG_reformer 667 C 8X 9 EX*M 10 EX_CH*M Comp-O2-1 DH water 0.369 803 4 86.9 1.0 bar Electrolyser 13.12 1.7 0.80 0 802 2 86.9 1.0 bar DH water 0.93 Steam reformer 0.02 NG_reformer O2 11 EX_PH*M 0.0 MW 1 0.906 86.9 kg/s 2.1 0.277 0.3 31.05 0.711 86.9 kg/s 0.0 0.002 12 C 13 C/EX SAND 2E-05 55 C Electro-cool 3 4 1.0 bar 2.1 kg/s 2 4 1.0 bar 0.3 kg/s 50 C Electro-cool Comp-O2-2 0.0 MW 3 Reformat 0.0 0.171 403 2 10.0 bar 0.0 kg/s 0.0 0 Ash 0.6 0.445 83 1.0 bar 4 0.6 kg/s 14 C/M O2 0.113 7 4 0.113 0.90 2.1 1.0 bar 0.277 2.1 kg/s 90 C Comp-O2-1 0.113 5 2 2.1 1.0 bar 0.277 2.1 kg/s 90 C Comp-O2-1 DH water Gas 0.113 90 C Electrolyser 0.0 -0 6 1.0 bar 4 0.0 kg/s 12.64 90 C Electrolyser H2 O2 2E-04 401 2 0.0 1.0 bar 4E-04 0.0 kg/s 90 C SAND 0.001 6E-04 402 4 0.94 6E-04 0.0 10.0 bar 0.001 0.0 kg/s 431 C 431 10.0 bar 4 0.0 kg/s 0.02 950 C NG_reformer 0.00 850 C NG_reformer 0.0 0.019 441 10.0 bar 2 0.0 kg/s 0.002 950 C Heatex-O2 Gasifier 304 0.0 MW SAND 0 800 C Gasifier 0.0 0.029 5.0 33 2 1.0 bar Steam 32 18.1 23.26 1.0 bar 801 2 14.3 0.117 1.0 bar 14.3 kg/s 15 4 4.6 2.112 1.0 bar 4.6 kg/s Heatsink-H2 -0 90 C Split-O2-2 O2 0.90 Comp-H2 Comp-O2-2 Comp-O2-2 432 2 0.0 0.05 10.0 bar 0.0 kg/s 0.0 0.00 0.97 Heatex-O2 SAND 11 6.416 5.0 kg/s Heatex-GG-st 4 18.1 kg/s 0 50 C 0 60 C 0.0 MW 322 12.64 0.0 MW 9 Comp-CO2 0.005 950 C 730 C SAND 7 0.11 730 C Heatex-GG-DH Cleaner SAND 0.0 SAND 4E-05 0.0 MW 7 Heatex-NG 0.89 10 Gasifier 11.7 255.5 10 18.2 234.8 Gasifier 10 GG2 0.11 0.78 1.0 bar 1.5 18.2 kg/s 800 C 10 18.2 233.7 11 2 1.0 bar 18.2 kg/s 761 C Heatex-GG-st 0.11 0.98 10 23.1 18.2 220.5 12 2 0.00 0.74 1.0 bar 2.4 18.2 kg/s 130 C Heatex-GG-DH 10 18.2 219.9 13 2 1.0 bar 18.2 kg/s 60 C 1.00 Gas cleaner 9.6 13.6 218.8 14 1.0 bar 0.00 Heatsink 12.64 12.64 511 2 0.3 1.0 bar 31.05 0.3 kg/s 90 C Heatsink-H2 0.019 503 4 0.0 19.8 bar SAND 0.003 0.002 502 4 0.002 0.001 501 2 0.93 0.0 19.8 bar 0.0 1.0 bar CO2 0.015 411 2 NG0.0 10.0 bar 0.173 0.0 kg/s 25 C Heatex-NG 451 Heatex-NG SAND 0.0 0.102 10.0 bar 0.0 13 0.02 0.89 0 434 Water 2 0.0 10.0 bar 82 1.0 bar Heatex-GG-O2 Heatex-GG-st Heatex-GG-DH SAND 9 Cleaner 4 13.6 kg/s 0.166 0.0 kg/s 0.007 0.0 kg/s 0.005 0.0 kg/s 2 0.0 kg/s 1E-05 0.0 kg/s 2 11.7 kg/s 0.11 9 2 Heatex-GG-O2 18.1 10.23 0 21 4 9.6 60 C 259 C 279 C 15 C 0.01 950 C 107 C 6.99 120 C 2.1 1.0 bar SAND 5 31 1.0 bar 0.0 1.0 bar Cleaner 12.64 512 2 27.37 524 4 13.9 261 Mixer-CO2-NG Comp-CO2 Comp-CO2 Heatex-H2O Pres-sep-3 Gasifier H2O [mass-%] = 0.05 Dry-wood 1.127 2.1 kg/s 790 C Gasifier 2 18.1 kg/s 0.079 120 C Heatex-GG-st 4E-18 0.0 kg/s 60 C 521 Heatex-GG-DH 2 13.9 249.8 1.0 bar 13.9 kg/s 0.3 31.05 1.0 bar 0.3 kg/s 90 C 13.9 260.8 19.8 bar 13.9 kg/s 305 C 531 2 27.39 19.8 bar 13.9 kg/s 304 C 1E-04 422 2 Water 0.0 10.0 bar 1E-05 0.0 kg/s 0.0 Heatex-H2O 0.00 0.74 SAND 15 0 453 Water 4 Steam 811 14.3 0.498 1.0 bar 22.23 63 C Comp-GG-H2-1 Comp-GG-H2-1 8.4 MW 11 Mixer-GG-H2 Comp-GG-H2-2 37.6 23.31 Syngas-cool1 33 C Heatex-H2O 0.0 2E-05 10.0 bar 0.0 kg/s 4 14.3 kg/s 0.93 SAND 8.391 571 1.0 bar Syngas-cool1 Comp-NG_ref 109 C 0.00 90 C 25.2 37.6 21.3 6 37.6 kg/s SAND 21 0.0 MW 5 0.0 Heatex-H2O 0.0 0.046 0.0 13.1 16.84 Heatex-GG-DH 13.9 257.6 563 1.0 bar 0.17 200 C 6.0 SAND 0.002 0.0 0.094 0.0 0.046 0.0 0.018 Steam_dryer Biomass (dry) 34 1.0 bar 522 6.0 bar 2 37.6 kg/s Syngas-cool1 0.17 0.82 452 10.0 bar 433 10.0 bar 442 10.0 bar 0.45 105.4 35 4 1.0 bar SAND 1 0.45 29.8 Steam dryer 6.99 0.45 94.9 34 2 1.0 bar 4 13.1 kg/s 0.077 730 C Split-steam2 2 13.9 kg/s 25.2 304 C Cooler-GG-H2 0.16 120 C Cooler-GG-H2 6.0 0.17 0.82 25.20 523 2 13.9 6.0 bar 0.93 27.37 561 2 0.164 37.6 21.32 1.0 bar 37.6 kg/s 120 C 0 541 4 0.0 19.8 bar 6E-18 0.0 kg/s 130 C Water Reformat 0.017 462 2 0.017 0.0 19.8 bar 0.16 0.0 kg/s 0.017 461 2 0.93 0.0 10.0 bar 0.158 0.0 kg/s 2 0.0 kg/s 0.01 109 C Mixer-NG_ref 2 0.0 kg/s 0.005 107 C Mixer-NG_ref 2 0.0 kg/s 0.002 483 C Mixer-NG_ref 59.71 105.4 kg/s 65.17 94.9 kg/s Cooler-GG-H2 37.6 23.29 255.2 13.9 kg/s Syngas-cool1 13.9 258.6 Syngas-cool1 250 C 154 C 120 C 22.2 256.3 278 C SAND 19 571 1.0 bar 130 C Comp-GG-H2-2 532 19.8 bar Mixer-CO2-NG Comp-NG_ref Steam_dryer 81 1.0 bar Steam_dryer 4 37.6 kg/s Comp-GG-H2-2 2 13.9 kg/s 2 6.86 22.2 kg/s 15 C Steam 0.17 200 C Cooler-GG-H2 6.1 MW SAND 13 6.098 27.39 130 C Comp-syngas1 Comp-syngas1 Component information Technical lifetime = O&M = 15 years 0.02 of the componentprice per year Operating hours = 8000 Exergy Steam DH-condenser Steam_dryer Biomass (wet) 5.6 3.144 41 1.0 bar 2 5.6 kg/s Steam 0.93 29.55 13.9 264.2 533 65.2 bar 4 13.9 kg/s Syngas 29.55 304 C 6.1 MW SAND 15 6.102 Electrolyser Comp-H2 Comp-O2-1 Node before component 1 2 5 Component type Electrolyser Compressor Compressor DNA name ELECTROLYSER COMPRE_1 COMPRE_1 Specific price 1.52 mio. kr/MWe 4.50 mio. kr/MW 4.50 mio. kr/MW Price [mio. kr] 60 0 0 Total price [mio. kr] 78 0 0 C [kr/s] 0.18 0.00 0.00 Input: NG Biomass Power* Total power * for electrolyser 0 MW 256 MW 40 MW 65 MW Output: Methanol DH Oxygen Syngas 231 MW 12 MW 0 MW 8 MW SAND 79 0.024 120 C 52.4 32.45 set_temp-2 Gasifier 9 Gasifier GASIFI_3 3.80 mio. kr/MW-biomass 815 1059 2.45 DH-condenser 0.73 12.9 0.41 811 12 DH condenser0.41 86.9 1.0 bar 581 2 0.24 1.0 bar 52.4 kg/s 200 C Steam 0.26 571 8 Heatex-GG-O2 Heatex-GG-st Heatex-GG-DH 10 11 12 Heat exchanger Heat exchanger Heat exchanger HEATEX_2 HEATEX_2 GASCOOL2 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 1 9 1 1 12 1 0.00 0.03 0.00 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 78% (with power for electrolyser) 72% (with total power) 78% 5.6 0.219 3.035 86.9 kg/s DH-cooler DH-cooler 57.9 1.0 bar Cleaner 13 Gas cleaner GASCLE_2 0.00 mio. kr/(kg/s)-gas 0 0 0.00 42 1.0 bar 90 C SAND 25 35.88 57.9 kg/s Steam_dryer 34 Steam dryer DRYER_04 4.10 mio. kr/(kg/s)-evaporated 43 56 0.13 4 5.6 kg/s 0 95 C DH-condenser DH-condenser 439.6 15.36 811 1.0 bar 0.010 811 6 49.8 1.0 bar 1.739 49.8 kg/s 0.48 8.3 0 804 2 DH cooler DH water 0.01 49.8 1.0 bar 0.408 49.8 kg/s 1.0 0.639 0.252 562 2 57.9 1.0 bar 200 C Syngas-cool2 9.2 0.26 0.91 Syngas-cool2 SAND 23 DH-condenser Comp-O2-2 Heatex-O2 41 401 402 Heat exchanger Compressor Heat exchanger HEATEX_1 COMPRE_1 HEATEX_4 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0.40 mio. kr/MW-transferred 5 0 0 7 0 0 0.02 0.00 0.00 Energy Water 2 439.6 kg/s 0.48 90 C DH DH water 90 C DH-cooler 35 6 52.4 29.67 1.0 bar 52.4 kg/s 50 C DH-cooler 571 1.0 bar 10 1.0 kg/s 0.00 225 C Cond-steam-1 32.81 57.9 kg/s 120 C Syngas-cool2 534 2 12.4 260.7 65.2 bar 12.4 kg/s 0 551 4 1.6 65.2 bar 0.138 1.6 kg/s 135 C NG_reformer Heatex-NG Water Heatex-H2O Comp-NG_ref Comp-CO2 403 411 422 461 501 NG reformer Heat exchanger Heat exchanger Compressor Compressor STEAM_REFORMER GASCOOL2 GASCOOL2 COMPRE_1 COMPRE_1 1.05 mio. kr/MW-NG 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 4.50 mio. kr/MW 0 0 0 0 0 0 0 0 0 0 0.00 0.00 0.00 0.00 0.00 Input: NG Biomass Power* Total power 0MW 214 MW 40 MW 65 MW Output: Methanol DH Oxygen Syngas 205 MW 74 MW 0 MW 7 MW Energy content in DH water = 74 MW 0.24 120 C DH-cooler Steam 29.55 135 C Comp-syngas2 Syngas-cool2 Heatsink-H2 Comp-GG-H2-1 511 521 Heat exchanger Compressor HEATSNK0 COMPRE_1 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0 38 0 49 0.00 0.11 * for electrolyser Urenhed: 0.008 % Methanol loss in distillation [%] = 1.0 Methanol molar-% = 99.99 Water / 671 1.0 0.566 1.0 bar 0.93 Comp-syngas2 30.82 3.6 MW 17 SAND 3.586 12.4 264.1 Cooler-GG-H2 Comp-GG-H2-2 Syngas-cool1 Comp-syngas1 522 523 531 532 Heat exchanger Compressor Heat exchanger Compressor GASCOOL2 COMPRE_1 GASCOOL2 COMPRE_1 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 0.40 mio. kr/MW-transferred 4.50 mio. kr/MW 2 27 2 27 3 36 3 36 0.01 0.08 0.01 0.08 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 81% (with power for electrolyser) 73% (with total power) 102% Methanol 2 1.0 kg/s 535 144.0 bar Syngas-cool2 533 Heat exchanger GASCOOL2 0.40 mio. kr/MW-transferred 4 5 0.01 0.00 120 C 2 12.4 kg/s Comp-syngas2 534 Compressor COMPRE_1 4.50 mio. kr/MW 16 21 0.05 Cond-steam-1 30.82 248 C Meoh-convert 601 Meoh converter MEOH_CONVERTER ##### mio. kr/(kmol/s-syngas) 254 330 0.76 Gas composition at specific nodes (mol-%) 31.41 10.3 231.1 set-M Preheater-sy 602 Heat exchanger GASCOOL4 0.40 mio. kr/MW-transferred 2 3 0.01 793 794 3.5 bar 10.3 kg/s 601 42.2 416.8 144.0 bar Condenser-1 Syngas Condenser 640 643 Heat exchanger Heat exchanger GASCOOL4 GASCOOL4 0.40 mio. kr/MW-transferred 0.40 mio. kr/MW-transferred 3 2 4 3 0.01 0.01 Node 10 3 15 431 534 601 602 640 643 605 15 23 33 35 41 43 39 37 M-factor 1.78 4 100 C 2 42.2 kg/s Comp-recirc 605 Compressor COMPRE_1 4.50 mio. kr/MW 1 1 0.00 Species Split-meoh1 127.3 41.7 936.6 Steam 0 682 4 51 235 C Meoh-convert feed_Water Cond-steam-1 625 671 Distillation column Heat exchanger DISTILLATION_STAGE* HEATEX_1 23.52 mio. kr/(kg/s-feed) 0.40 mio. kr/MW-transferred 254 0 330 0 0.76 0.00 1 3 H2 N2 45.61 0.21 0.00 57.70 60.67 45.40 22.81 24.39 28.19 30.00 0.00 0.00 0.23 2.28 3.30 3.53 4.08 4.34 791 3.5 bar 17.8 30.6 bar Cond-steam-2 685 Heat exchanger HEATSNK0 0.40 mio. kr/MW-transferred 13 17 0.04 4 CO 32.23 0.00 22.49 34.03 20.51 5.24 5.60 6.47 6.89 792 41.7 kg/s 18.23 17.8 kg/s DH-cooler 804 Heat exchanger HEATEX_1 0.40 mio. kr/MW-transferred 3 4 0.01 6 CO2 9.40 99.97 5.09 0.03 26.44 40.34 43.14 49.87 53.07 Heatsourc-DH 4 100 C Cond-steam-1 235 C Heatsourc-DH 806 Heat exchanger HEATSRC0 0.40 mio. kr/MW-transferred 17 22 0.05 7 H2O-G 12.29 0.00 14.17 4.78 2.41 1.49 0.97 0.20 0.01 SAND 390 Cond-meoh SAND 35 Convert-cool * The distillation column is composed of 9 H2S 0.00 0.03 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.051 811 10 42.7 254.6 1.0 bar 0.051 0.70 0 806 2 DH water 254.6 1.0 bar 0 683 2 0.1 30.6 bar 0.2 0.00 0.81 0 684 4 0.1 30.6 bar Water 0 681 2 17.8 30.6 bar 33.1 Meoh-convert Methanol 1.00 SAND converter 51 311 Total several DISTILLATION_STAGE's 1601 2055 4.82 11 36 40 CH4 AR CH3OH 0.15 0.10 0.00 0.00 0.00 0.00 0.55 0.00 0.00 0.16 0.11 0.00 1.58 2.30 2.46 1.09 1.58 1.69 0.29 22.94 18.23 2.84 1.96 6.39 3.02 2.08 0.59 8.895 254.6 kg/s 90 C 2.085 254.6 kg/s 50 C 0.115 0.1 kg/s 235 C 0.025 0.1 kg/s 220 C 3.92 17.8 kg/s 220 C 602 42.2 400.7 139.0 bar 607 29.8 150.7 144.0 bar Input prices GG H2S NG_ref-cool Syngas-loop1 Syngas-meoh- Syngas-loop2 Syngas-3 Syngas-meoh Syngas-loop3 95.88 Heatsourc-DH 127.3 31.4 705.5 783 41.7 946.3 Heatsourc-DH 3.5 bar Cond-steam-1 Cond-steam-1 Convert-cool 2 51 42.2 kg/s 235 C 2 20 29.8 kg/s 225 C Input Electric power Price 324 kr/GJ Output cost Comparable fuel prices 781 3.5 bar 784 41.7 kg/s 17.7 18.12 Preheater-sy Mixer-syn_re Mechanical power 341 kr/GJ Output Cost flow Cost (exergy) Cost (energy) Cost (mass) Cost (volume) Fuel Price (exergy) Price (volume) 782 31.4 kg/s 4 100 C 685 30.6 bar 6.1 Preheater-sy NG 93 kr/GJ Methanol 31.4 kr/s 136 kr/GJ 153 kr/GJ 3.05 kr/kg 2.4 kr/l Methanol (commercial) 142 kr/GJ 2.5 kr/l 2 100 C Dis_stage_17 2 17.7 kg/s 20 606 2 20 0.60 SAND 29 Biomass 32 kr/GJ Oxygen 0.0 kr/s 407 kr/GJ - kr/GJ 0.05 kr/kg - kr/l Petrol 187 kr/GJ 6.6 kr/l Dis_stage_17 0 235 C Comp-recirc 20 29.8 144.0 bar 39.3 336.1 DH water 0 kr/ton Syngas 1.0 kr/s 132 kr/GJ - kr/GJ 0.66 kr/kg - kr/l Crude oil 58 kr/GJ 2.2 kr/l Cond-steam-2 0.1 MW 19 0.90 148.9 29.8 kg/s 640 139.0 bar 91 7.937 2.9 61.49 Water 32 kr/ton DH water 0.5 kr/s 31 kr/GJ 6 kr/GJ 0.00 kr/kg - kr/l Ethanol 100 kr/GJ 2.4 kr/l 0 681 4 SAND 0.116 63 C 2 39.3 kg/s 621 139.0 bar CO2 114 kr/ton Water 0 kr/s - kr/GJ - kr/GJ - kr/kg - kr/l Distillation column 142 0.78 Feed 17.7 3.895 30.6 bar 17.7 kg/s 220 C Preheater-sy 43.39 181 C Condenser-1 8.5 631 2.9 kg/s 4 181 C Preheater-sy Nomenclature: Cond-steam-2 2.95 0.50 If methanol and DH share the plant costs Condenser-1 94.1 16.18 621 631 4 (methanol and DH are the only products from the plant) - 14 705 706 21 3.5 bar 2 2.95 705 706 4 3.5 bar 6 SAND 31 33.6 207.8 643 139.0 bar 2 33.6 kg/s 6 139.0 bar 124 5.7 kg/s 134 C and the DH cost is fixed corresponding to the DH price: Output Cost flow Cost Methanol 21.8 kr/s 95 kr/Gjex Electrical power Node nr Pressure Transferred heat [MW] 115 21.5 kg/s 24 4.4 kg/s Condenser 27.21 134 C Preheater-sy DH water 11.1 kr/s 150 kr/Gjen Mass flow 124 C 124 C SAND 33 Condenser Temperature Dis_stage_1 0.01 811 8 34.0 1.0 bar Reboil-meoh2 5.7 0.01 0.40 0 805 2 DH water 34.0 1.0 bar Mechanical power 10 14.27 22.0 106.1 1.189 34.0 kg/s 0.279 34.0 kg/s 2.943 4.4 21.39 707 3.5 bar Cond-steam-2 90 C 19.69 605 2 50 C 699 3.5 bar 0.25 708 22.0 kg/s SAND 393 Condenser 29.8 139.0 bar 1.6 7.83 Condenser 700 4.4 kg/s 4 124 C 148.8 29.8 kg/s 611 139.0 bar 96.8 6.483 2.2 48.98 2 124 C Water / Methanol Methanol molar-% = 13.17 0 693 694 0 3.5 bar 2 0.5 kg/s Dis_stage_1 4 11.33 695 696 17 3.5 bar 82 17.0 kg/s 2 32.9 11.37 0.64 11.37 705 706 17 3.5 bar 91 17.0 kg/s 4 30.6 625 635 11 3.5 bar 2 Methanol molar-% = 94 60 C Comp-recirc Methanol/ 4 1.6 kg/s 1.036 60 C Syngas Split-syngas 621 139.0 bar 631 2.2 kg/s 4 60 C Preheater-sy Reboil-meoh2 Heat Exergy efficiency [-] 64 C set-x-2 124 C Reboil-meoh1 124 C Reboil-meoh1 234 10.8 kg/s 101 C meas_flow Methanol mass flow = 10.4 kg/s water

23. Flowsheets for metanolanlæg - til den termoøkonomiske analyse. Flowsheet 1/5: Flow-parametre: P, m& , t Komponent-parameter: ηex Flowsheet 2/5: Flow-parametre: m& , h, x Komponent-parameter: Ċi, dest Flowsheet 3/5: Flow-parametre: eex, m, eex,ch,m, eex,ph,m Komponent-parameter: Ċp, dest Flowsheet 4/5: Flow-parametre: Ėex, Ėex, ch, Ėex, ph Komponent-parameter: Ėex, dest Flowsheet 5/5: Flow-parametre: Ċ, cex, cm Komponent-parameter: Ż

Page 1 and 2: Design og modellering af metanolanl

Page 3 and 4: 2 Resumé I forbindelse med DONG En

Page 5 and 6: 4 Indholdsfortegnelse 1 Abstract...

Page 7 and 8: 5 Indledning Baggrunden for dette p

Page 9 and 10: 7 Design og statisk modellering af

Page 11 and 12: Brint er specielt fordelagtig til m

Page 13 and 14: Ligning 7.1: Den specifikke varmeka

Page 15 and 16: DNA-navn: DRYER_04 Forgasser Forgas

Page 17 and 18: T Fordampning Pinch points Figur 7.

Page 19 and 20: Massestrøm af Metanol/vand-blandin

Page 21 and 22: Parameter Værdi Komponenter Evt. k

Page 23 and 24: 7.2 Anlægskonfigurationer Den opby

Page 25 and 26: 7.3 Økonomi For at kunne vurdere o

Page 27 and 28: Input-priser Kilde Elektricitet 18

Page 29 and 30: 7.4 Termoøkonomisk analyse Der er

Page 31 and 32: Komponent Produkt(er) Spild Elektro

Page 33 and 34: Tabet i fysisk exergi forekommer ho

Page 35 and 36: Anlæg 1 Total: 320 MWex (292 MW) 7

Page 37 and 38: antagelse, da naturgasnettet er try

Page 39 and 40: 246 562 112 Anlæg 1 Total: 1222 mi

Page 41 and 42: Brændsel Pris Kilde [kr/L] [kr/GJe

Page 43 and 44: Metanolomkostning [kr/GJex] 500 450

Page 45 and 46: 7.5.2 Parametervariation Nedenfor e

Page 47 and 48: Udkondenseret metanol [%] 100 95 90

Page 49 and 50: Metanolrenhed efter destillation [m

Page 51 and 52: vandkoncentrationen i syngassen fal

Page 53 and 54: Metanolexergivirkningsgrad [%] 73 7

Page 55 and 56: Metanolrenhed efter destillation [m

Page 57 and 58: Dette betyder at den metanolholdige

Page 59 and 60: Atmosfærisk forgasning (1 bar) Try

Page 61 and 62: 7.6 Diskussion I parametervariation

Page 63 and 64: 7.6.2 Alternative anlægsdesign Ned

Page 65 and 66: 8 Benyttelse af underjordiske gasla

Page 67 and 68: 8.2 Scenarier Der er undersøgt 2 s

Page 69 and 70: Ligning 8.5: Reference-el-omkostnin

Page 71 and 72: Ligning 8.13: Tidskonstant for lage

Page 73 and 74: Brintlagerbeholdning [MWh] 3000 250

Page 75 and 76: Brintlagerbeholdning [MWh] 400 350

Page 77 and 78: den time, hvor regulatorligningen b

Page 79 and 80: El-pris-funktionen [kr/MWh] 500 450

Page 81 and 82: Brintlagerbeholdning [MWh] 100 90 8

Page 83 and 84: Omkostninger [%] 100 90 80 70 60 50

Page 85 and 86: Sparede omkostninger [%] 30 25 20 1

Page 87 and 88: selvstændig investering og de omko

Page 89 and 90: Tilbagebetalingstid (beregnet ud fr

Page 91 and 92: Sparede omkostninger i nutidsværdi

Page 93 and 94: Tilbagebetalingstid [år] 15 10 5 0

Page 95 and 96: 8.4 Diskussion Resultaterne præsen

Page 97 and 98: El-pris [kr/Mwh] 400 350 300 250 20

Page 99 and 100: 9 Konklusion I den første del af r

Page 101 and 102: http://www.energyserver.net/ET1/Def

Page 103 and 104: 11 Nomenklaturliste c omkostning pe

Page 105 and 106: Design og modellering af metanolanl

Page 107 and 108: 25. Flowsheets for metanolanlæg -

Page 109 and 110: 2. Forgasserpris - Choren Choren In

Page 111 and 112: 4. El-afgifter og -tariffer GE-NET

Page 113 and 114: 6. Naturgasafgifter - DONG Energy N

Page 115 and 116: 8. Benzinforbrug til vejtransport E

Page 117 and 118: 10. Benzinafgift Benzinafgifter fra

Page 119 and 120: 12. Metanolpris Metanolpriser fra M

Page 121 and 122: Methanex Non-Discounted Reference P

Page 127 and 128: 14. Metanolproduktion, NZIC New Zea

Page 129 and 130: Maui Gas Supply Kapuni Gas Supply N

Page 131 and 132: Gas metering and letdown The proces

Page 133 and 134: Methanol Distillation Crude methano

Page 135 and 136: Product Gasoline Pipeline (250 mm N

Page 137 and 138: steam, preheat the reactants (steam

Page 139 and 140: As it is very difficult to separate

Page 141 and 142: Operational processes A schematic l

Page 143 and 144: The reaction of the synthesis gas c

Page 145 and 146: Figure 15 - Flowsheet of the MTG pr

Page 147 and 148: 15. Metanolproduktion, Nykomb Nykom

Page 149 and 150: NYKOMB SYNERGETICS 2. Methanol Plan

Page 151 and 152: NYKOMB SYNERGETICS 6. Investment Es

Page 153 and 154: NYKOMB SYNERGETICS 9. Logistics and

Page 155 and 156: 16. Metanolproduktion, Wikipedia Wi

Page 157 and 158: 18. Flowsheet for et metanolanlæg

Page 159 and 160: 20. Flowsheet for metanolanlæg - u

Page 161 and 162: 21. Flowsheet for metanolanlæg - t

Page 163: 22. Flowsheet for metanolanlæg - t

Page 167 and 168: 0 1 1 1 P 2 M type NOD* 2 1 type NO


Page 171 and 172: 24. Flowsheets for metanolanlæg -







Page 185 and 186: 27. Flowsheet for metanolanlæg - f

Page 187 and 188: 28. Flowsheet for metanolanlæg - f

Page 189 and 190: 29. Matlab-kode til Scenarie 1

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Page 213 and 214: 32. DNA-kode for metanolanlæg

Page 215 and 216: metanolanlaeg.dna d:/DTU/Eksamenspr

Page 217 and 218: metanolanlaeg.dna d:/DTU/Eksamenspr

Page 219 and 220: 33. Dokumentation for tilføjede DN

Page 221 and 222: 17.121.4 Conditions ˙m1 > 0 ˙m2 <

Page 223 and 224: 9. - 10. - 11. - 12. - 13. - 14. -

Page 225 and 226: 17.123 GASIFI_3_VENZIN Gasifier wit

Page 227 and 228: 13. - 14. - 15. - 16. - 17. - 18. -

Page 229 and 230: 17.124 GASCLE_2 Syngas cleaning. Th

Page 231 and 232: 38. Compound number 39. Compound nu

Page 233 and 234: 43. - 44. - 45. - 46. - 47. - 48. -

Page 235 and 236: 17.124.5 Example struc Cleaner GASC

Page 237 and 238: 10. - 11. - 12. - 13. - 17.125.4 Co

Page 239 and 240: 7. - 8. - 9. - 10. - 11. - 12. - 13


Page 243 and 244: 11. - 12. - 13. - 14. - 15. - 16. -

Page 245 and 246: 17.128 SET_M Utility component for

Page 247 and 248: 4. - 5. - 6. - 7. - 8. - 9. - 10. -



Page 253 and 254: 17.131.2 Equations Number of equati

Page 255 and 256: 17.132 EL-MOTOR Motor with efficien

Page 257 and 258: 8. - 9. - 17.133.3 Conditions ˙m1

Page 259 and 260: 17.135 MIXER_03 Mixer for ideal gas

Page 261 and 262: 33. - 34. - 35. - 36. - 37. - 38. -

Page 263 and 264: 17.137 SET_X Utility component for


Page 267 and 268: 17.140 SET_FLOW Utillity component

Page 269 and 270: 17.142 SET_TEMP2 Utillity component

Page 271 and 272: 34. Tilføjede komponenter til DNA

Page 273 and 274: VEnzin.for c:/dna/source/ C C Param

Page 275 and 276: VEnzin.for c:/dna/source/ CA ANTED

Page 277 and 278: VEnzin.for c:/dna/source/ IF (MDOT(

Page 279 and 280: VEnzin.for c:/dna/source/ MMVAR(1)

Page 281 and 282: VEnzin.for c:/dna/source/ ENDDO DO

Page 283 and 284: VEnzin.for c:/dna/source/ $fluid O2

Page 285 and 286: VEnzin.for c:/dna/source/ C−−

Page 287 and 288: VEnzin.for c:/dna/source/ CA FKOMP

Page 289 and 290: VEnzin.for c:/dna/source/ ENDDO NIN

Page 291 and 292: VEnzin.for c:/dna/source/ C Subrout

Page 293 and 294: VEnzin.for c:/dna/source/ CALL STAT

Page 295 and 296: VEnzin.for c:/dna/source/ CA 3: Flu

Page 297 and 298: VEnzin.for c:/dna/source/ C C C M_B

Page 299 and 300: VEnzin.for c:/dna/source/ C C SETFL

Page 301 and 302: VEnzin.for c:/dna/source/ C C GASCO

Page 303 and 304: VEnzin.for c:/dna/source/ RES(5) =

Page 305 and 306: VEnzin.for c:/dna/source/ c c c E2=

Page 307 and 308: VEnzin.for c:/dna/source/ C C HEATE

Page 309 and 310: VEnzin.for c:/dna/source/ $ ’$\\d

Page 311 and 312: VEnzin.for c:/dna/source/ c 1 = Wat

Page 313 and 314: VEnzin.for c:/dna/source/ CA 4: Fin

Page 315 and 316: VEnzin.for c:/dna/source/ CL K_MED

Page 317 and 318: VEnzin.for c:/dna/source/ CA MEDIE

Page 319 and 320: VEnzin.for c:/dna/source/ CA −4 :

Page 321 and 322: VEnzin.for c:/dna/source/ C ENDDO E

Page 323 and 324: VEnzin.for c:/dna/source/ MEDIE(2)

Page 325 and 326: VEnzin.for c:/dna/source/ C C 400 C

Page 327 and 328: VEnzin.for c:/dna/source/ GOTO 9999

Page 329 and 330: VEnzin.for c:/dna/source/ MEDIE(1)


Page 333 and 334: VEnzin.for c:/dna/source/ RES(1) =



Page 339 and 340: 35. Metanol (fluid) til DNA - Fortr

Page 341 and 342: methanol.for d:/DTU/Eksamensprojekt









methanol

exchanger

output

goto

component

electrolyser

compressor

input

gasifier

syngas

modellering

bilag

etd.dtu.dk

Design og modellering af metanolanlæg til VEnzin-visionen Bilag

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Design og modellering af metanolanlæg til VEnzin-visionen Bilag Design og modellering af metanolanlæg til VEnzin-visionen Bilag