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 5 Component cost flow 2 2.4 kg/s 39.7 MW 201 2 0.0 kg/s 0.0 10.0 bar NG 6 EX_CH * Number of decimals Electrolyser 0.076 15 C SAND 39.71 0.00 850 C 0.176 0.0 kg/s 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 0.45 105.4 Steam_dryer Biomass (dry) SAND 1 35 4 0.45 29.8 0.45 34 2 1.0 bar Steam dryer 6.99 94.9 1.0 bar 34 1.0 bar 4 13.1 kg/s 0.077 730 C Split-steam2 522 6.0 bar 2 13.9 kg/s 25.2 304 C Cooler-GG-H2 2 37.6 kg/s 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 Syngas-cool1 561 2 0.164 37.6 21.32 1.0 bar 37.6 kg/s 120 C 0.17 0.82 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 452 10.0 bar 2 0.0 kg/s 0.01 109 C Mixer-NG_ref 433 10.0 bar 2 0.0 kg/s 0.005 107 C Mixer-NG_ref 442 10.0 bar 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-% = 93.8 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
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 4.5 -0 4.3 7.757 4H 3 0 4Exergy destruction cost flow - based on specific cost of output 1 1.0 bar Electrolyser 423 10.0 bar 19.51 412 2 5EX 5 Component cost flow 2 4.5 kg/s 76.1 MW 201 2 4.3 kg/s 4.3 10.0 bar NG 6 EX_CH * Number of decimals Electrolyser 0.145 15 C SAND 76.14 0.16 850 C 223.6 4.3 kg/s 7 EX_PH SAND 301 Electrolyser NG_reformer 667 C 8X 9 EX*M 10 EX_CH*M Comp-O2-1 DH water 0.28 803 4 19.4 1.0 bar Electrolyser 25.16 3.2 0.80 0 802 2 19.4 1.0 bar DH water 0.93 Steam reformer 21.04 NG_reformer O2 11 EX_PH*M 0.0 MW 1 0.675 19.4 kg/s 4.0 0.531 0.5 59.53 0.159 19.4 kg/s 4.0 3.055 12 C 13 C/EX SAND 1E-08 90 C Electro-cool 3 4 1.0 bar 4.0 kg/s 2 4 1.0 bar 0.5 kg/s 50 C Electro-cool Comp-O2-2 1.4 MW 3 Reformat 12.7 217 403 2 10.0 bar 4.0 kg/s 0.0 0 Ash 0.0 2E-04 83 1.0 bar 4 0.0 kg/s 14 C/M O2 5E-05 7 4 5E-05 0.90 0.0 1.0 bar 1E-04 0.0 kg/s 90 C Comp-O2-1 5E-05 5 2 0.0 1.0 bar 1E-04 0.0 kg/s 90 C Comp-O2-1 DH water Gas 0.22 90 C Electrolyser 0.0 1E-37 6 1.0 bar 4 0.0 kg/s 24.66 90 C Electrolyser H2 O2 0.22 401 2 4.0 1.0 bar 0.531 4.0 kg/s 90 C SAND 1.377 0.708 402 4 0.94 0.708 4.0 10.0 bar 1.824 4.0 kg/s 431 C 431 10.0 bar 4 12.7 kg/s 21.04 950 C NG_reformer 0.71 850 C NG_reformer 1.4 24.49 441 10.0 bar 2 1.4 kg/s 2.375 950 C Heatex-O2 Gasifier 304 0.0 MW SAND 0 800 C Gasifier 0.0 5E-05 0.0 33 2 1.0 bar Steam 32 0.0 0.009 1.0 bar 801 2 0.0 4E-05 1.0 bar 0.0 kg/s 15 4 0.0 1E-05 1.0 bar 0.0 kg/s Heatsink-H2 6E-38 90 C Split-O2-2 O2 0.90 Comp-H2 Comp-O2-2 Comp-O2-2 432 2 3.7 63.04 10.0 bar 3.7 kg/s 1.8 0.71 0.97 Heatex-O2 SAND 11 0.001 0.0 kg/s Heatex-GG-st 4 0.0 kg/s 0 50 C 0 60 C 0.0 MW 322 24.66 0.0 MW 9 Comp-CO2 6.113 950 C 730 C SAND 7 0.00 730 C Heatex-GG-DH Cleaner SAND 0.0 SAND 9E-05 1.7 MW 7 Heatex-NG 0.89 0 Gasifier 0.0 0.115 0 0.0 0.104 Gasifier 10 GG2 0.00 0.78 1.0 bar 0.0 0.0 kg/s 800 C 0 0.0 0.104 11 2 1.0 bar 0.0 kg/s 752 C Heatex-GG-st 0.00 0.99 0 0.0 0.0 0.099 12 2 0.00 0.74 1.0 bar 0.0 0.0 kg/s 130 C Heatex-GG-DH 0 0.0 0.099 13 2 1.0 bar 0.0 kg/s 60 C 1.00 Gas cleaner 0.0 0.0 0.099 14 1.0 bar 0.00 Heatsink 24.66 24.66 511 2 0.5 1.0 bar 59.53 0.5 kg/s 90 C Heatsink-H2 23.43 503 4 18.5 19.7 bar SAND 1.703 1.364 502 4 1.364 0.76 501 2 0.93 6.7 19.7 bar 6.7 1.0 bar CO2 19.5 411 2 NG4.3 10.0 bar 219 4.3 kg/s 25 C Heatex-NG 451 Heatex-NG SAND 7.6 129.5 10.0 bar 8.8 13 19.51 0.89 0 434 Water 2 0.3 10.0 bar 82 1.0 bar Heatex-GG-O2 Heatex-GG-st Heatex-GG-DH SAND 9 Cleaner 4 0.0 kg/s 206.4 18.5 kg/s 4.589 6.7 kg/s 3.009 6.7 kg/s 2 7.6 kg/s 0.016 0.3 kg/s 2 0.0 kg/s 0.00 9 2 Heatex-GG-O2 0.0 0.004 0 21 4 0.0 60 C 255 C 279 C 15 C 12.56 950 C 107 C 0.00 120 C 0.0 1.0 bar SAND 5 31 1.0 bar 0.0 1.0 bar Cleaner 24.66 512 2 25.88 524 4 19.0 268.3 Mixer-CO2-NG Comp-CO2 Comp-CO2 Heatex-H2O Pres-sep-3 Gasifier H2O [mass-%] = 0.05 Dry-wood 5E-04 0.0 kg/s 790 C Gasifier 2 0.0 kg/s 3E-04 120 C Heatex-GG-st 2E-22 0.0 kg/s 60 C 521 Heatex-GG-DH 2 0.5 59.63 1.0 bar 0.5 kg/s 0.5 59.53 1.0 bar 0.5 kg/s 90 C 0.5 62.38 19.7 bar 0.5 kg/s 395 C 531 2 49.3 19.7 bar 19.0 kg/s 278 C 0.138 422 2 Water 4.3 10.0 bar 0.014 4.3 kg/s 17.9 Heatex-H2O 0.16 0.74 SAND 15 0 453 Water 4 Steam 811 0.0 2E-04 1.0 bar 24.67 90 C Comp-GG-H2-1 Comp-GG-H2-1 1.4 MW 11 Mixer-GG-H2 Comp-GG-H2-2 40.8 25.27 Syngas-cool1 33 C Heatex-H2O 0.5 0.029 10.0 bar 0.5 kg/s 4 0.0 kg/s 0.93 SAND 1.416 571 1.0 bar Syngas-cool1 Comp-NG_ref 109 C 0.00 90 C 25.17 6.9 3.9 6 40.8 kg/s SAND 21 2.9 MW 5 7.0 Heatex-H2O 3.4 57.92 1.4 0.0 0.007 Heatex-GG-DH 0.5 60.94 563 1.0 bar 2.02 200 C 6.5 SAND 2.878 7.0 119 3.4 57.92 1.4 23.22 0.00 0.0 Steam_dryer Biomass (dry) SAND 1 35 4 0.46 0.0 0.00 34 2 1.0 bar Steam dryer 0.00 0.0 1.0 bar 34 1.0 bar 4 0.0 kg/s 3E-04 730 C Split-steam2 522 3.8 bar 2 0.5 kg/s 25.17 278 C Cooler-GG-H2 2 6.9 kg/s 0.34 120 C Cooler-GG-H2 1.1 0.34 0.85 25.17 523 2 0.5 3.8 bar 0.94 25.88 Syngas-cool1 561 2 2.021 40.8 23.12 1.0 bar 40.8 kg/s 120 C 2.03 0.85 0 541 4 0.0 19.7 bar 1E-17 0.0 kg/s 130 C Water Reformat 22.06 462 2 22.06 11.8 19.7 bar 202.6 11.8 kg/s 21.04 461 2 0.93 11.8 10.0 bar 199.9 11.8 kg/s 452 10.0 bar 2 7.0 kg/s 12.56 109 C Mixer-NG_ref 433 10.0 bar 2 3.4 kg/s 6.113 107 C Mixer-NG_ref 442 10.0 bar 2 1.4 kg/s 2.375 483 C Mixer-NG_ref 0.028 0.0 kg/s 0.03 0.0 kg/s Cooler-GG-H2 6.9 4.264 60.51 0.5 kg/s Syngas-cool1 19.0 265.8 Syngas-cool1 249 C 154 C 120 C 0.0 0.115 271 C SAND 19 571 1.0 bar 130 C Comp-GG-H2-2 532 19.7 bar Mixer-CO2-NG Comp-NG_ref Steam_dryer 81 1.0 bar Steam_dryer 4 6.9 kg/s Comp-GG-H2-2 2 19.0 kg/s 2 0.003 0.0 kg/s 15 C Steam 0.34 200 C Cooler-GG-H2 2.0 MW SAND 13 1.998 49.3 130 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) 0.0 0.002 41 1.0 bar 2 0.0 kg/s Steam 0.93 51.65 19.0 271.9 533 59.4 bar 4 19.0 kg/s Syngas 51.65 278 C 6.6 MW SAND 15 6.616 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] 116 0 0 Total price [mio. kr] 150 0 0 C [kr/s] 0.35 0.00 0.00 Input: NG Biomass Power* Total power * for electrolyser 219 MW 0 MW 76 MW 99 MW Output: Methanol DH Oxygen Syngas 231 MW 11 MW 0 MW 19 MW SAND 79 2E-04 120 C 100.2 62.05 set_temp-2 Gasifier 9 Gasifier GASIFI_3 3.80 mio. kr/MW-biomass 0 0 0.00 DH-condenser 0.91 0.0 0.28 811 12 DH condenser0.28 19.4 1.0 bar 581 1.0 bar 2 100.2 kg/s 4.97 200 C Steam 2.56 571 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 0 0 0 0 0 0 0.00 0.00 0.00 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 78% (with power for electrolyser) 73% (with total power) 82% 0.0 1E-04 0.677 19.4 kg/s DH-cooler DH-cooler 51.5 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 31.9 51.5 kg/s Steam_dryer 34 Steam dryer DRYER_04 4.10 mio. kr/(kg/s)-evaporated 0 0 0.00 4 0.0 kg/s 0 95 C DH-condenser DH-condenser 421.9 14.74 811 1.0 bar 0.019 811 6 95.3 1.0 bar 3.328 95.3 kg/s 0.48 16.0 DH cooler 0.02 0 804 2 DH water 95.3 1.0 bar 0.78 95.3 kg/s 1.0 0.639 2.551 562 2 51.5 1.0 bar 200 C Syngas-cool2 8.2 2.56 0.88 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 0 6 1 0 8 1 0.00 0.02 0.00 Energy Water 2 421.9 kg/s 0.36 90 C DH DH water 90 C DH-cooler 100.2 56.74 35 1.0 bar 6 100.2 kg/s 50 C DH-cooler 571 1.0 bar 10 1.0 kg/s 0.05 225 C Cond-steam-1 29.18 51.5 kg/s 120 C Syngas-cool2 534 2 18.0 268.8 59.4 bar 18.0 kg/s 0 551 4 1.0 59.4 bar 0.095 1.0 kg/s 141 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 219 4 7 13 8 285 5 9 17 10 0.66 0.01 0.02 0.04 0.02 Input: NG Biomass Power* Total power 210 MW 0 MW 76 MW 99 MW Output: Methanol DH Oxygen Syngas 205 MW 71 MW 0 MW 15 MW Energy content in DH water = 71 MW 4.97 120 C DH-cooler Steam 51.65 141 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 6 0 8 0.00 0.02 * for electrolyser Urenhed: 0.105 % Methanol loss in distillation [%] = 1.0 Methanol molar-% = 99.89 Water / 671 1.0 0.566 1.0 bar 0.93 Comp-syngas2 53.45 5.1 MW 17 SAND 5.075 18.0 273.5 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 0 9 3 30 1 12 3 39 0.00 0.03 0.01 0.09 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 72% (with power for electrolyser) 66% (with total power) 94% Methanol 2 1.0 kg/s 535 144.0 bar Syngas-cool2 533 Heat exchanger GASCOOL2 0.40 mio. kr/MW-transferred 3 4 0.01 0.05 120 C 2 18.0 kg/s Comp-syngas2 534 Compressor COMPRE_1 4.50 mio. kr/MW 23 30 0.07 Cond-steam-1 53.45 260 C Meoh-convert 601 Meoh converter MEOH_CONVERTER ##### mio. kr/(kmol/s-syngas) 475 618 1.43 Gas composition at specific nodes (mol-%) 51.97 10.3 231.1 set-M Preheater-sy 602 Heat exchanger GASCOOL4 0.40 mio. kr/MW-transferred 6 8 0.02 793 794 3.5 bar 10.3 kg/s 601 96.3 629.5 144.0 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 7 3 9 0.01 0.02 Node 10 3 15 431 534 601 602 640 643 605 15 23 33 35 41 43 39 37 M-factor 1.45 4 100 C 2 96.3 kg/s Comp-recirc 605 Compressor COMPRE_1 4.50 mio. kr/MW 1 2 0.00 Species Split-meoh1 168.7 33.5 750.2 Steam 0 682 4 131 235 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 327 0 425 0 0.98 0.00 1 3 H2 N2 45.98 0.25 0.00 57.70 61.60 40.52 25.25 26.87 27.93 30.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 791 3.5 bar 14.8 30.6 bar Cond-steam-2 685 Heat exchanger HEATSNK0 0.40 mio. kr/MW-transferred 11 14 0.03 4 CO 42.73 0.00 22.49 16.51 7.02 1.92 2.04 2.12 2.28 792 33.4 kg/s 15.14 14.8 kg/s DH-cooler 804 Heat exchanger HEATEX_1 0.40 mio. kr/MW-transferred 6 8 0.02 6 CO2 5.24 0.00 5.09 15.32 47.39 53.36 56.77 59.02 63.39 Heatsourc-DH 4 100 C Cond-steam-1 235 C Heatsourc-DH 806 Heat exchanger HEATSRC0 0.40 mio. kr/MW-transferred 14 18 0.04 7 H2O-G 5.21 0.00 14.17 6.18 2.09 5.95 3.06 1.57 0.05 SAND 390 Cond-meoh SAND 35 Convert-cool * The distillation column is composed of 9 H2S 0.00 ##### 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.041 811 10 34.2 204.2 1.0 bar 0.041 0.70 0 806 2 DH water 204.2 1.0 bar 0 683 2 0.1 30.6 bar 0.2 0.05 0.81 0 684 4 0.1 30.6 bar Water 0 681 2 14.8 30.6 bar 27.5 Meoh-convert Methanol 1.00 SAND converter 132 311 Total several DISTILLATION_STAGE's 1298 1662 3.91 11 36 40 CH4 AR CH3OH 0.48 0.12 0.00 0.00 0.00 0.00 0.55 0.00 0.00 0.40 0.00 0.00 2.67 3.19 0.00 0.00 0.32 10.32 3.40 0.00 7.86 3.53 0.00 5.82 3.80 0.00 0.48 7.133 204.2 kg/s 90 C 1.672 204.2 kg/s 50 C 0.115 0.1 kg/s 235 C 0.025 0.1 kg/s 220 C 3.256 14.8 kg/s 220 C 602 96.3 616.3 139.0 bar 607 78.3 357.5 144.0 bar Input prices GG H2S NG_ref-cool Syngas-loop1 Syngas-meoh- Syngas-loop2 Syngas-3 Syngas-meoh Syngas-loop3 116.7 Heatsourc-DH 168.7 23.1 519 783 33.5 757.9 Heatsourc-DH 3.5 bar Cond-steam-1 Cond-steam-1 Convert-cool 2 132 96.3 kg/s 235 C 2 77 78.3 kg/s 225 C Input Electric power Price 324 kr/GJ Output cost Comparable fuel prices 781 3.5 bar 784 33.4 kg/s 14.7 15.03 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 23.1 kg/s 4 100 C 685 30.6 bar 16.0 Preheater-sy NG 93 kr/GJ Methanol 52.0 kr/s 225 kr/GJ 254 kr/GJ 5.05 kr/kg 4.0 kr/l Methanol (commercial) 142 kr/GJ 2.5 kr/l 2 100 C Dis_stage_17 2 14.7 kg/s 77 606 2 77 0.86 SAND 29 Biomass 32 kr/GJ Oxygen 0.0 kr/s 414 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 77 78.3 144.0 bar 91.5 541 DH water 0 kr/ton Syngas 4.1 kr/s 219 kr/GJ - kr/GJ 0.98 kr/kg - kr/l Crude oil 58 kr/GJ 2.2 kr/l Cond-steam-2 0.3 MW 19 0.90 352.6 78.3 kg/s 640 139.0 bar 49 15.06 4.9 69.64 Water 32 kr/ton DH water 0.4 kr/s 24 kr/GJ 5 kr/GJ 0.00 kr/kg - kr/l Ethanol 100 kr/GJ 2.4 kr/l 0 681 4 SAND 0.292 63 C 2 91.5 kg/s 621 139.0 bar CO2 114 kr/ton Water 0 kr/s - kr/GJ - kr/GJ - kr/kg - kr/l Distillation column 172 0.69 Feed 14.7 3.232 30.6 bar 14.7 kg/s 220 C Preheater-sy 117 166 C Condenser-1 6.4 631 4.9 kg/s 4 166 C Preheater-sy Nomenclature: Cond-steam-2 0.61 1.03 If methanol and DH share the plant costs Condenser-1 59.3 10.87 621 631 4 (methanol and DH are the only products from the plant) - 3 705 706 16 3.5 bar 2 0.61 705 706 3 3.5 bar 6 SAND 31 88.4 489 643 139.0 bar 2 88.4 kg/s 3 139.0 bar 50 3.1 kg/s 146 C and the DH cost is fixed corresponding to the DH price: Output Cost flow Cost Methanol 45.8 kr/s 198 kr/Gjex Electrical power Node nr Pressure Transferred heat [MW] 22 15.9 kg/s 4 3.0 kg/s Condenser 106.1 146 C Preheater-sy DH water 10.6 kr/s 150 kr/Gjen Mass flow 136 C 136 C SAND 33 Condenser Temperature Dis_stage_1 0.02 811 8 103.1 1.0 bar Reboil-meoh2 17.3 0.02 0.74 0 805 2 DH water 103.1 1.0 bar Mechanical power 10 3.185 19.5 14.31 3.601 103.1 kg/s 0.844 103.1 kg/s 0.605 3.0 2.217 707 3.5 bar Cond-steam-2 90 C 77.04 605 2 50 C 699 3.5 bar 0.25 708 19.5 kg/s SAND 393 Condenser 78.3 139.0 bar 4.1 18.54 Condenser 700 3.0 kg/s 4 136 C 352.4 78.3 kg/s 611 139.0 bar 77.9 25.02 5.9 114.4 2 136 C Water / Methanol Methanol molar-% = 1.65 0 693 694 4 3.5 bar 3 3.6 kg/s Dis_stage_1 4 2.58 695 696 13 3.5 bar 9 12.9 kg/s 2 27.3 2.613 0.69 2.613 705 706 13 3.5 bar 18 12.9 kg/s 4 50.95 625 635 14 3.5 bar 2 Methanol molar-% = 62.7 60 C Comp-recirc Methanol/ 4 4.1 kg/s 4.055 60 C Syngas Split-syngas 621 139.0 bar 631 5.9 kg/s 4 60 C Preheater-sy Reboil-meoh2 Heat Exergy efficiency [-] 64 C set-x-2 136 C Reboil-meoh1 136 C Reboil-meoh1 234 13.9 kg/s 104 C meas_flow Methanol mass flow = 10.4 kg/s water
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Design og modellering af metanolanl
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2 Resumé I forbindelse med DONG En
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4 Indholdsfortegnelse 1 Abstract...
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5 Indledning Baggrunden for dette p
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7 Design og statisk modellering af
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Brint er specielt fordelagtig til m
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Ligning 7.1: Den specifikke varmeka
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DNA-navn: DRYER_04 Forgasser Forgas
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T Fordampning Pinch points Figur 7.
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Massestrøm af Metanol/vand-blandin
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Parameter Værdi Komponenter Evt. k
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7.2 Anlægskonfigurationer Den opby
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7.3 Økonomi For at kunne vurdere o
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Input-priser Kilde Elektricitet 18
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7.4 Termoøkonomisk analyse Der er
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Komponent Produkt(er) Spild Elektro
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Tabet i fysisk exergi forekommer ho
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Anlæg 1 Total: 320 MWex (292 MW) 7
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antagelse, da naturgasnettet er try
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246 562 112 Anlæg 1 Total: 1222 mi
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Brændsel Pris Kilde [kr/L] [kr/GJe
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Metanolomkostning [kr/GJex] 500 450
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7.5.2 Parametervariation Nedenfor e
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Udkondenseret metanol [%] 100 95 90
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Metanolrenhed efter destillation [m
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vandkoncentrationen i syngassen fal
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Metanolexergivirkningsgrad [%] 73 7
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Metanolrenhed efter destillation [m
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Dette betyder at den metanolholdige
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Atmosfærisk forgasning (1 bar) Try
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7.6 Diskussion I parametervariation
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7.6.2 Alternative anlægsdesign Ned
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8 Benyttelse af underjordiske gasla
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8.2 Scenarier Der er undersøgt 2 s
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Ligning 8.5: Reference-el-omkostnin
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Ligning 8.13: Tidskonstant for lage
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Brintlagerbeholdning [MWh] 3000 250
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Brintlagerbeholdning [MWh] 400 350
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den time, hvor regulatorligningen b
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El-pris-funktionen [kr/MWh] 500 450
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Brintlagerbeholdning [MWh] 100 90 8
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Omkostninger [%] 100 90 80 70 60 50
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Sparede omkostninger [%] 30 25 20 1
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selvstændig investering og de omko
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Tilbagebetalingstid (beregnet ud fr
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Sparede omkostninger i nutidsværdi
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Tilbagebetalingstid [år] 15 10 5 0
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8.4 Diskussion Resultaterne præsen
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El-pris [kr/Mwh] 400 350 300 250 20
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9 Konklusion I den første del af r
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http://www.energyserver.net/ET1/Def
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11 Nomenklaturliste c omkostning pe
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Design og modellering af metanolanl
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25. Flowsheets for metanolanlæg -
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2. Forgasserpris - Choren Choren In
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4. El-afgifter og -tariffer GE-NET
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6. Naturgasafgifter - DONG Energy N
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8. Benzinforbrug til vejtransport E
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10. Benzinafgift Benzinafgifter fra
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12. Metanolpris Metanolpriser fra M
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Methanex Non-Discounted Reference P
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Page 131 and 132: Gas metering and letdown The proces
Page 133 and 134: Methanol Distillation Crude methano
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Page 137 and 138: steam, preheat the reactants (steam
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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
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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
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Page 173: 0 1 1 1 P 2 M type NOD* 1 1 type NO
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Page 189 and 190: 29. Matlab-kode til Scenarie 1
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Page 209 and 210: Sparede omkostninger i nutidsværdi
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Page 213 and 214: 32. DNA-kode for metanolanlæg
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17.123 GASIFI_3_VENZIN Gasifier wit
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13. - 14. - 15. - 16. - 17. - 18. -
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17.124 GASCLE_2 Syngas cleaning. Th
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38. Compound number 39. Compound nu
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43. - 44. - 45. - 46. - 47. - 48. -
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17.124.5 Example struc Cleaner GASC
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10. - 11. - 12. - 13. - 17.125.4 Co
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7. - 8. - 9. - 10. - 11. - 12. - 13
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17.126.4 Conditions ˙m1 > 0 ˙m2 <
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11. - 12. - 13. - 14. - 15. - 16. -
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17.128 SET_M Utility component for
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4. - 5. - 6. - 7. - 8. - 9. - 10. -
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17.129.4 Conditions ˙m1 > 0 ˙m2 <
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17.130.4 Conditions ˙m1 > 0 ˙m2 <
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17.131.2 Equations Number of equati
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17.132 EL-MOTOR Motor with efficien
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8. - 9. - 17.133.3 Conditions ˙m1
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17.135 MIXER_03 Mixer for ideal gas
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33. - 34. - 35. - 36. - 37. - 38. -
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17.137 SET_X Utility component for
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17.138.4 Conditions ˙m1 > 0 ˙m2 <
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17.140 SET_FLOW Utillity component
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17.142 SET_TEMP2 Utillity component
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34. Tilføjede komponenter til DNA
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VEnzin.for c:/dna/source/ C C Param
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VEnzin.for c:/dna/source/ CA ANTED
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VEnzin.for c:/dna/source/ IF (MDOT(
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VEnzin.for c:/dna/source/ MMVAR(1)
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VEnzin.for c:/dna/source/ ENDDO DO
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VEnzin.for c:/dna/source/ $fluid O2
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VEnzin.for c:/dna/source/ C−−
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VEnzin.for c:/dna/source/ CA FKOMP
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VEnzin.for c:/dna/source/ ENDDO NIN
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VEnzin.for c:/dna/source/ C Subrout
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VEnzin.for c:/dna/source/ CALL STAT
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VEnzin.for c:/dna/source/ CA 3: Flu
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VEnzin.for c:/dna/source/ C C C M_B
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VEnzin.for c:/dna/source/ C C SETFL
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VEnzin.for c:/dna/source/ C C GASCO
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VEnzin.for c:/dna/source/ RES(5) =
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VEnzin.for c:/dna/source/ c c c E2=
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VEnzin.for c:/dna/source/ C C HEATE
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VEnzin.for c:/dna/source/ $ ’$\\d
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VEnzin.for c:/dna/source/ c 1 = Wat
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VEnzin.for c:/dna/source/ CA 4: Fin
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VEnzin.for c:/dna/source/ CL K_MED
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VEnzin.for c:/dna/source/ CA MEDIE
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VEnzin.for c:/dna/source/ CA −4 :
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VEnzin.for c:/dna/source/ C ENDDO E
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VEnzin.for c:/dna/source/ MEDIE(2)
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VEnzin.for c:/dna/source/ C C 400 C
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VEnzin.for c:/dna/source/ GOTO 9999
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VEnzin.for c:/dna/source/ MEDIE(1)
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VEnzin.for c:/dna/source/ RES(1) =
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35. Metanol (fluid) til DNA - Fortr
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methanol.for d:/DTU/Eksamensprojekt
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Design og modellering af metanolanlæg til VEnzin-visionen Bilag

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