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 3.4 -0 1.9 3.399 4H 3 0 4Exergy destruction cost flow - based on specific cost of output 1 1.0 bar Electrolyser 423 10.0 bar 8.55 412 2 5EX 5 Component cost flow 2 3.4 kg/s 56.3 MW 201 2 1.9 kg/s 1.9 10.0 bar NG 6 EX_CH * Number of decimals Electrolyser 0.107 15 C SAND 56.34 0.07 850 C 97.97 1.9 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 0.381 803 4 78.5 1.0 bar Electrolyser 18.62 2.4 0.80 0 802 2 78.5 1.0 bar DH water 0.93 Steam reformer 9.22 NG_reformer O2 11 EX_PH*M 0.0 MW 1 0.927 78.5 kg/s 3.0 0.393 0.4 44.05 0.643 78.5 kg/s 1.8 1.339 12 C 13 C/EX SAND 1E-05 57 C Electro-cool 3 4 1.0 bar 3.0 kg/s 2 4 1.0 bar 0.4 kg/s 50 C Electro-cool Comp-O2-2 0.6 MW 3 Reformat 5.6 95.09 403 2 10.0 bar 1.8 kg/s 0.0 0 Ash 0.3 0.252 83 1.0 bar 4 0.3 kg/s 14 C/M O2 0.066 7 4 0.066 0.90 1.2 1.0 bar 0.16 1.2 kg/s 90 C Comp-O2-1 0.066 5 2 1.2 1.0 bar 0.16 1.2 kg/s 90 C Comp-O2-1 DH water Gas 0.161 90 C Electrolyser 0.0 9E-36 6 1.0 bar 4 0.0 kg/s 18.08 90 C Electrolyser H2 O2 0.095 401 2 1.8 1.0 bar 0.233 1.8 kg/s 90 C SAND 0.604 0.309 402 4 0.94 0.309 1.8 10.0 bar 0.799 1.8 kg/s 431 C 431 10.0 bar 4 5.6 kg/s 9.22 950 C NG_reformer 0.31 850 C NG_reformer 0.6 10.73 441 10.0 bar 2 0.6 kg/s 1.041 950 C Heatex-O2 Gasifier 304 0.0 MW SAND 0 800 C Gasifier 0.0 0.009 1.3 33 2 1.0 bar Steam 32 8.4 10.81 1.0 bar 801 2 6.8 0.056 1.0 bar 6.8 kg/s 15 4 0.0 0.016 1.0 bar 0.0 kg/s Heatsink-H2 4E-36 90 C Split-O2-2 O2 0.90 Comp-H2 Comp-O2-2 Comp-O2-2 432 2 1.6 27.62 10.0 bar 1.6 kg/s 0.8 0.31 0.97 Heatex-O2 SAND 11 1.707 1.3 kg/s Heatex-GG-st 4 8.4 kg/s 0 50 C 0 60 C 0.0 MW 322 18.08 0.0 MW 9 Comp-CO2 2.678 950 C 730 C SAND 7 0.06 730 C Heatex-GG-DH Cleaner SAND 0.0 SAND 6E-05 0.0 MW 7 Heatex-NG 0.89 5 Gasifier 6.6 144.7 5 8.9 131.6 Gasifier 10 GG2 0.07 0.78 1.0 bar 0.9 8.9 kg/s 800 C 5 8.9 130.9 11 2 1.0 bar 8.9 kg/s 752 C Heatex-GG-st 0.06 0.99 5 10.8 8.9 124.8 12 2 0.00 0.74 1.0 bar 1.1 8.9 kg/s 130 C Heatex-GG-DH 5 8.9 124.6 13 2 1.0 bar 8.9 kg/s 60 C 1.00 Gas cleaner 5.4 8.9 124.5 14 1.0 bar 0.00 Heatsink 18.08 18.08 511 2 0.4 1.0 bar 44.05 0.4 kg/s 90 C Heatsink-H2 9.671 503 4 5.2 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 8.545 411 2 NG1.9 10.0 bar 95.97 1.9 kg/s 25 C Heatex-NG 451 Heatex-NG SAND 3.3 56.74 10.0 bar 3.9 13 8.55 0.89 0 434 Water 2 0.1 10.0 bar 82 1.0 bar Heatex-GG-O2 Heatex-GG-st Heatex-GG-DH SAND 9 Cleaner 4 8.9 kg/s 88.77 5.2 kg/s 0.007 0.0 kg/s 0.005 0.0 kg/s 2 3.3 kg/s 0.007 0.1 kg/s 2 6.6 kg/s 0.07 9 2 Heatex-GG-O2 8.4 4.755 0 21 4 5.4 60 C 250 C 279 C 15 C 5.501 950 C 107 C 3.96 120 C 1.2 1.0 bar SAND 5 31 1.0 bar 0.0 1.0 bar Cleaner 18.08 512 2 26.82 524 4 14.4 264.3 Mixer-CO2-NG Comp-CO2 Comp-CO2 Heatex-H2O Pres-sep-3 Gasifier H2O [mass-%] = 0.05 Dry-wood 0.653 1.2 kg/s 790 C Gasifier 2 8.4 kg/s 0.043 120 C Heatex-GG-st -0 0.0 kg/s 60 C 521 Heatex-GG-DH 2 9.2 168.4 1.0 bar 9.2 kg/s 0.4 44.05 1.0 bar 0.4 kg/s 90 C 9.2 175.7 19.8 bar 9.2 kg/s 320 C 531 2 36.49 19.8 bar 14.4 kg/s 294 C 0.061 422 2 Water 1.9 10.0 bar 0.006 1.9 kg/s 7.8 Heatex-H2O 0.07 0.74 SAND 15 0 453 Water 4 Steam 811 6.8 0.237 1.0 bar 23.50 68 C Comp-GG-H2-1 Comp-GG-H2-1 5.1 MW 11 Mixer-GG-H2 Comp-GG-H2-2 36.2 22.42 Syngas-cool1 33 C Heatex-H2O 0.2 0.013 10.0 bar 0.2 kg/s 4 6.8 kg/s 0.93 SAND 5.071 571 1.0 bar Syngas-cool1 Comp-NG_ref 109 C 0.00 90 C 25.3 22.7 12.89 6 36.2 kg/s SAND 21 1.3 MW 5 3.1 Heatex-H2O 1.5 25.38 0.6 7.1 9.101 Heatex-GG-DH 9.2 173.1 563 1.0 bar 0.19 200 C 5.8 SAND 1.267 3.1 52.16 1.5 25.38 0.6 10.17 0.31 62.1 Steam_dryer Biomass (dry) SAND 1 35 4 0.46 16.9 0.31 34 2 1.0 bar Steam dryer 3.96 56.1 1.0 bar 34 1.0 bar 4 7.1 kg/s 0.047 730 C Split-steam2 522 5.5 bar 2 9.2 kg/s 25.3 294 C Cooler-GG-H2 2 22.7 kg/s 0.12 120 C Cooler-GG-H2 3.6 0.12 0.83 25.30 523 2 9.2 5.5 bar 0.93 26.82 Syngas-cool1 561 2 0.186 36.2 20.51 1.0 bar 36.2 kg/s 120 C 0.19 0.83 0 541 4 0.0 19.8 bar -0 0.0 kg/s 130 C Water Reformat 9.669 462 2 9.669 5.2 19.8 bar 88.77 5.2 kg/s 9.22 461 2 0.93 5.2 10.0 bar 87.59 5.2 kg/s 452 10.0 bar 2 3.1 kg/s 5.501 109 C Mixer-NG_ref 433 10.0 bar 2 1.5 kg/s 2.678 107 C Mixer-NG_ref 442 10.0 bar 2 0.6 kg/s 1.041 483 C Mixer-NG_ref 35.17 62.1 kg/s 38.2 56.1 kg/s Cooler-GG-H2 22.7 14.09 171.7 9.2 kg/s Syngas-cool1 14.4 262 Syngas-cool1 250 C 154 C 120 C 12.6 145.2 271 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 22.7 kg/s Comp-GG-H2-2 2 14.4 kg/s 2 3.886 12.6 kg/s 15 C Steam 0.12 200 C Cooler-GG-H2 4.3 MW SAND 13 4.28 36.49 130 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) 4.6 2.629 41 1.0 bar 2 4.6 kg/s Steam 0.93 38.57 14.4 267.5 533 62.2 bar 4 14.4 kg/s Syngas 38.57 294 C 5.9 MW SAND 15 5.869 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] 86 0 0 Total price [mio. kr] 111 0 0 C [kr/s] 0.26 0.00 0.00 Input: NG Biomass Power* Total power * for electrolyser 96 MW 145 MW 56 MW 79 MW Output: Methanol DH Oxygen Syngas 231 MW 12 MW 0 MW 13 MW SAND 79 0.024 120 C 53.5 33.11 set_temp-2 Gasifier 9 Gasifier GASIFI_3 3.80 mio. kr/MW-biomass 461 600 1.39 DH-condenser 0.74 10.8 0.42 811 12 DH condenser0.42 78.5 1.0 bar 581 2 0.28 1.0 bar 53.5 kg/s 200 C Steam 0.23 571 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 4 0 0 6 1 0.00 0.01 0.00 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 78% (with power for electrolyser) 72% (with total power) 80% 4.6 0.183 2.743 78.5 kg/s DH-cooler DH-cooler 42.5 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 26.35 42.5 kg/s Steam_dryer 34 Steam dryer DRYER_04 4.10 mio. kr/(kg/s)-evaporated 24 32 0.07 4 4.6 kg/s 0 95 C DH-condenser DH-condenser 430.0 15.02 811 1.0 bar 0.010 811 6 50.8 1.0 bar 1.776 50.8 kg/s 0.48 8.5 0 804 2 DH cooler DH water 0.01 50.8 1.0 bar 0.416 50.8 kg/s 1.0 0.639 0.219 562 2 42.5 1.0 bar 200 C Syngas-cool2 6.8 0.23 0.87 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 4 3 0 6 4 0 0.01 0.01 0.00 Energy Water 2 430.0 kg/s 0.49 90 C DH DH water 90 C DH-cooler 35 6 53.5 30.28 1.0 bar 53.5 kg/s 50 C DH-cooler 571 1.0 bar 10 1.0 kg/s 0.01 225 C Cond-steam-1 24.1 42.5 kg/s 120 C Syngas-cool2 534 2 13.9 264.9 62.2 bar 13.9 kg/s 0 551 4 0.6 62.2 bar 0.049 0.6 kg/s 136 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 96 2 3 6 0 125 2 4 7 0 0.29 0.00 0.01 0.02 0.00 Input: NG Biomass Power* Total power 92 MW 121 MW 56 MW 79 MW Output: Methanol DH Oxygen Syngas 205 MW 72 MW 0 MW 11 MW Energy content in DH water = 72 MW 0.28 120 C DH-cooler Steam 38.57 136 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 23 0 30 0.00 0.07 * for electrolyser Urenhed: 0.023 % Methanol loss in distillation [%] = 1.0 Methanol molar-% = 99.98 Water / 671 1.0 0.566 1.0 bar 0.93 Comp-syngas2 40.01 4.1 MW 17 SAND 4.068 13.9 268.6 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 1 19 2 26 2 25 3 34 0.00 0.06 0.01 0.08 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 76% (with power for electrolyser) 70% (with total power) 99% 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 0.01 120 C 2 13.9 kg/s Comp-syngas2 534 Compressor COMPRE_1 4.50 mio. kr/MW 18 24 0.06 Cond-steam-1 40.01 253 C Meoh-convert 601 Meoh converter MEOH_CONVERTER ##### mio. kr/(kmol/s-syngas) 327 424 0.98 Gas composition at specific nodes (mol-%) 39.74 10.3 231.1 set-M Preheater-sy 602 Heat exchanger GASCOOL4 0.40 mio. kr/MW-transferred 4 5 0.01 793 794 3.5 bar 10.3 kg/s 601 59.3 519.3 144.0 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 4 3 5 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 1.67 4 100 C 2 59.3 kg/s Comp-recirc 605 Compressor COMPRE_1 4.50 mio. kr/MW 1 1 0.00 Species Split-meoh1 148 38.4 860.6 Steam 0 682 4 82 235 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 270 0 351 0 0.81 0.00 1 3 H2 N2 45.98 0.25 0.00 57.70 60.63 42.70 24.36 25.92 27.89 30.00 0.00 0.00 0.12 1.00 1.32 1.40 1.51 1.62 791 3.5 bar 17.1 30.6 bar Cond-steam-2 685 Heat exchanger HEATSNK0 0.40 mio. kr/MW-transferred 13 16 0.04 4 CO 42.73 0.00 22.49 29.16 14.45 3.27 3.47 3.74 4.02 792 38.4 kg/s 17.55 17.1 kg/s DH-cooler 804 Heat exchanger HEATEX_1 0.40 mio. kr/MW-transferred 3 4 0.01 6 CO2 5.24 0.00 5.09 4.47 35.29 46.38 49.35 53.11 57.12 Heatsourc-DH 4 100 C Cond-steam-1 235 C Heatsourc-DH 806 Heat exchanger HEATSRC0 0.40 mio. kr/MW-transferred 16 20 0.05 7 H2O-G 5.21 0.00 14.17 5.12 2.13 2.93 1.70 0.62 0.02 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 0.047 811 10 39.2 234.0 1.0 bar 0.047 0.70 0 806 2 DH water 234.0 1.0 bar 0 683 2 0.1 30.6 bar 0.2 0.01 0.81 0 684 4 0.1 30.6 bar Water 0 681 2 17.1 30.6 bar 31.8 Meoh-convert Methanol 1.00 SAND converter 83 311 Total several DISTILLATION_STAGE's 1423 1826 4.28 11 36 40 CH4 AR CH3OH 0.48 0.12 0.00 0.00 0.00 0.00 0.55 0.00 0.00 0.44 0.06 0.00 3.62 4.77 5.08 0.48 0.63 0.67 0.33 16.33 12.39 5.47 0.73 6.94 5.88 0.78 0.56 8.175 234.0 kg/s 90 C 1.916 234.0 kg/s 50 C 0.115 0.1 kg/s 235 C 0.025 0.1 kg/s 220 C 3.774 17.1 kg/s 220 C 602 59.3 503.9 139.0 bar 607 45.4 251 144.0 bar Input prices GG H2S NG_ref-cool Syngas-loop1 Syngas-meoh- Syngas-loop2 Syngas-3 Syngas-meoh Syngas-loop3 108.3 Heatsourc-DH 148 28.1 629.5 783 38.4 869.6 Heatsourc-DH 3.5 bar Cond-steam-1 Cond-steam-1 Convert-cool 2 83 59.3 kg/s 235 C 2 42 45.4 kg/s 225 C Input Electric power Price 324 kr/GJ Output cost Comparable fuel prices 781 3.5 bar 784 38.4 kg/s 17.0 17.43 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 28.1 kg/s 4 100 C 685 30.6 bar 9.5 Preheater-sy NG 93 kr/GJ Methanol 39.7 kr/s 172 kr/GJ 194 kr/GJ 3.86 kr/kg 3.0 kr/l Methanol (commercial) 142 kr/GJ 2.5 kr/l 2 100 C Dis_stage_17 2 17.0 kg/s 42 606 2 42 0.77 SAND 29 Biomass 32 kr/GJ Oxygen 0.0 kr/s 410 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 42 45.4 144.0 bar 55.7 431 DH water 0 kr/ton Syngas 2.2 kr/s 167 kr/GJ - kr/GJ 0.91 kr/kg - kr/l Crude oil 58 kr/GJ 2.2 kr/l Cond-steam-2 0.2 MW 19 0.90 248.1 45.4 kg/s 640 139.0 bar 78 11.42 3.6 69.19 Water 32 kr/ton DH water 0.5 kr/s 32 kr/GJ 7 kr/GJ 0.00 kr/kg - kr/l Ethanol 100 kr/GJ 2.4 kr/l 0 681 4 SAND 0.176 63 C 2 55.7 kg/s 621 139.0 bar CO2 114 kr/ton Water 0 kr/s - kr/GJ - kr/GJ - kr/kg - kr/l Distillation column 155 0.73 Feed 17.0 3.749 30.6 bar 17.0 kg/s 220 C Preheater-sy 71.13 170 C Condenser-1 6.6 631 3.6 kg/s 4 170 C Preheater-sy Nomenclature: Cond-steam-2 1.21 0.78 If methanol and DH share the plant costs Condenser-1 84.1 13.67 621 631 4 (methanol and DH are the only products from the plant) - 7 705 706 19 3.5 bar 2 1.21 705 706 3 3.5 bar 6 SAND 31 51.6 346.2 643 139.0 bar 2 51.6 kg/s 4 139.0 bar 82 4.1 kg/s 142 C and the DH cost is fixed corresponding to the DH price: Output Cost flow Cost Methanol 31.6 kr/s 137 kr/Gjex Electrical power Node nr Pressure Transferred heat [MW] 49 18.5 kg/s 9 3.2 kg/s Condenser 57.46 142 C Preheater-sy DH water 10.8 kr/s 150 kr/Gjen Mass flow 132 C 132 C SAND 33 Condenser Temperature Dis_stage_1 0.01 811 8 59.9 1.0 bar Reboil-meoh2 10.0 0.01 0.58 0 805 2 DH water 59.9 1.0 bar Mechanical power 10 6.915 19.8 40.63 2.091 59.9 kg/s 0.49 59.9 kg/s 1.2 3.2 6.628 707 3.5 bar Cond-steam-2 90 C 41.48 605 2 50 C 699 3.5 bar 0.25 708 19.7 kg/s SAND 393 Condenser 45.4 139.0 bar 2.4 13.05 Condenser 700 3.2 kg/s 4 132 C 247.9 45.4 kg/s 611 139.0 bar 91.4 13.8 3.9 82.48 2 132 C Water / Methanol Methanol molar-% = 5.16 0 693 694 1 3.5 bar 2 1.2 kg/s Dis_stage_1 4 5.716 695 696 15 3.5 bar 32 15.4 kg/s 2 31.6 5.754 0.67 5.754 705 706 15 3.5 bar 41 15.4 kg/s 4 38.88 625 635 11 3.5 bar 2 Methanol molar-% = 84.5 60 C Comp-recirc Methanol/ 4 2.4 kg/s 2.183 60 C Syngas Split-syngas 621 139.0 bar 631 3.9 kg/s 4 60 C Preheater-sy Reboil-meoh2 Heat Exergy efficiency [-] 64 C set-x-2 132 C Reboil-meoh1 132 C Reboil-meoh1 234 11.5 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 5.8 -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 5.8 kg/s 96.7 MW 201 2 0.0 kg/s 0.0 10.0 bar NG 6 EX_CH * Number of decimals Electrolyser 0.184 15 C SAND 96.65 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 0.592 803 4 115.3 1.0 bar Electrolyser 31.94 4.1 0.80 0 802 2 115.3 1.0 bar DH water 0.93 Steam reformer 0.02 NG_reformer O2 11 EX_PH*M 0.0 MW 1 1.439 115.3 kg/s 5.1 0.674 0.6 75.57 0.944 115.3 kg/s 0.0 0.002 12 C 13 C/EX SAND 2E-05 59 C Electro-cool 3 4 1.0 bar 5.1 kg/s 2 4 1.0 bar 0.6 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 0.5 0.357 83 1.0 bar 4 0.5 kg/s 14 C/M O2 0.093 7 4 0.093 0.90 1.7 1.0 bar 0.227 1.7 kg/s 90 C Comp-O2-1 0.093 5 2 1.7 1.0 bar 0.227 1.7 kg/s 90 C Comp-O2-1 DH water Gas 0.277 90 C Electrolyser 3.4 0.447 6 1.0 bar 4 3.4 kg/s 31.07 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 0.011 1.9 33 2 1.0 bar Steam 32 11.9 15.28 1.0 bar 801 2 9.6 0.079 1.0 bar 9.6 kg/s 15 4 0.0 0.023 1.0 bar 0.0 kg/s Heatsink-H2 0.184 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 2.414 1.9 kg/s Heatex-GG-st 4 11.9 kg/s 0 50 C 0 60 C 0.0 MW 322 31.07 0.0 MW 9 Comp-CO2 0.005 950 C 730 C SAND 7 0.07 730 C Heatex-GG-DH Cleaner SAND 0.0 SAND 1E-04 0.0 MW 7 Heatex-NG 0.89 8 Gasifier 9.4 204.7 8 12.5 186.1 Gasifier 10 GG2 0.09 0.78 1.0 bar 1.2 12.5 kg/s 800 C 8 12.5 185.2 11 2 1.0 bar 12.5 kg/s 752 C Heatex-GG-st 0.07 0.99 8 15.2 12.5 176.5 12 2 0.00 0.74 1.0 bar 1.6 12.5 kg/s 130 C Heatex-GG-DH 8 12.5 176.1 13 2 1.0 bar 12.5 kg/s 60 C 1.00 Gas cleaner 7.7 12.5 176.1 14 1.0 bar 0.00 Heatsink 31.07 31.07 511 2 0.6 1.0 bar 75.57 0.6 kg/s 90 C Heatsink-H2 0.019 503 4 0.0 18.5 bar SAND 0.002 0.002 502 4 0.002 0.001 501 2 0.93 0.0 18.5 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 12.5 kg/s 0.165 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 9.4 kg/s 0.09 9 2 Heatex-GG-O2 11.9 6.724 0 21 4 7.7 60 C 250 C 272 C 15 C 0.01 950 C 107 C 5.60 120 C 1.7 1.0 bar SAND 5 31 1.0 bar 0.0 1.0 bar Cleaner 31.07 512 2 43.56 524 4 13.2 261.9 Mixer-CO2-NG Comp-CO2 Comp-CO2 Heatex-H2O Pres-sep-3 Gasifier H2O [mass-%] = 0.05 Dry-wood 0.924 1.7 kg/s 790 C Gasifier 2 11.9 kg/s 0.051 120 C Heatex-GG-st 5E-20 0.0 kg/s 60 C 521 Heatex-GG-DH 2 13.2 251.4 1.0 bar 13.2 kg/s 0.6 75.57 1.0 bar 0.6 kg/s 90 C 13.2 261.7 18.5 bar 13.2 kg/s 303 C 531 2 43.58 18.5 bar 13.2 kg/s 303 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 9.6 0.336 1.0 bar 38.74 69 C Comp-GG-H2-1 Comp-GG-H2-1 7.8 MW 11 Mixer-GG-H2 Comp-GG-H2-2 35.7 22.12 Syngas-cool1 33 C Heatex-H2O 0.0 2E-05 10.0 bar 0.0 kg/s 4 9.6 kg/s 0.93 SAND 7.805 571 1.0 bar Syngas-cool1 Comp-NG_ref 109 C 0.00 90 C 41.51 35.7 20.21 6 35.7 kg/s SAND 21 0.0 MW 5 0.0 Heatex-H2O 0.0 0.046 0.0 10.0 12.87 Heatex-GG-DH 13.2 258.7 563 1.0 bar 0.16 200 C 5.7 SAND 0.002 0.0 0.094 0.0 0.046 0.0 0.018 0.37 87.8 Steam_dryer Biomass (dry) SAND 1 35 4 0.46 23.9 0.37 34 2 1.0 bar Steam dryer 5.60 79.4 1.0 bar 34 1.0 bar 4 10.0 kg/s 0.058 730 C Split-steam2 522 5.7 bar 2 13.2 kg/s 41.51 303 C Cooler-GG-H2 2 35.7 kg/s 0.15 120 C Cooler-GG-H2 5.7 0.16 0.82 41.51 523 2 13.2 5.7 bar 0.93 43.56 Syngas-cool1 561 2 0.153 35.7 20.23 1.0 bar 35.7 kg/s 120 C 0.16 0.82 0 541 4 0.0 18.5 bar 7E-18 0.0 kg/s 130 C Water Reformat 0.017 462 2 0.017 0.0 18.5 bar 0.16 0.0 kg/s 0.017 461 2 0.92 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 49.74 87.8 kg/s 54.02 79.4 kg/s Cooler-GG-H2 35.7 22.09 256.4 13.2 kg/s Syngas-cool1 13.2 259.6 Syngas-cool1 240 C 154 C 120 C 17.8 205.3 271 C SAND 19 571 1.0 bar 130 C Comp-GG-H2-2 532 18.5 bar Mixer-CO2-NG Comp-NG_ref Steam_dryer 81 1.0 bar Steam_dryer 4 35.7 kg/s Comp-GG-H2-2 2 13.2 kg/s 2 5.495 17.8 kg/s 15 C Steam 0.16 200 C Cooler-GG-H2 5.8 MW SAND 13 5.785 43.58 130 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) 6.6 3.718 41 1.0 bar 2 6.6 kg/s Steam 0.93 45.63 13.2 265 533 60.6 bar 4 13.2 kg/s Syngas 45.63 303 C 5.8 MW SAND 15 5.789 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] 147 0 0 Total price [mio. kr] 191 0 0 C [kr/s] 0.44 0.00 0.00 Input: NG Biomass Power* Total power * for electrolyser 0 MW 205 MW 97 MW 121 MW Output: Methanol DH Oxygen Syngas 231 MW 12 MW 0 MW 11 MW SAND 79 0.028 120 C 38.7 23.99 set_temp-2 Gasifier 9 Gasifier GASIFI_3 3.80 mio. kr/MW-biomass 653 848 1.96 DH-condenser 0.75 15.2 0.64 811 12 DH condenser0.64 115.3 1.0 bar 581 2 0.17 1.0 bar 38.7 kg/s 200 C Steam 0.16 571 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 6 1 1 8 1 0.00 0.02 0.00 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 76% (with power for electrolyser) 71% (with total power) 78% 6.6 0.259 4.029 115.3 kg/s DH-cooler DH-cooler 35.7 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 22.12 35.7 kg/s Steam_dryer 34 Steam dryer DRYER_04 4.10 mio. kr/(kg/s)-evaporated 35 45 0.10 4 6.6 kg/s 0 95 C DH-condenser DH-condenser 450.0 15.72 811 1.0 bar 0.007 811 6 36.8 1.0 bar 1.286 36.8 kg/s 0.48 6.2 0 804 2 DH cooler DH water 0.01 36.8 1.0 bar 0.301 36.8 kg/s 1.0 0.639 0.153 562 2 35.7 1.0 bar 200 C Syngas-cool2 5.7 0.16 0.82 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 6 0 0 8 0 0 0.02 0.00 0.00 Energy Water 2 450.0 kg/s 0.71 90 C DH DH water 90 C DH-cooler 35 6 38.7 21.94 1.0 bar 38.7 kg/s 50 C DH-cooler 571 1.0 bar 10 1.0 kg/s 0.00 225 C Cond-steam-1 20.23 35.7 kg/s 120 C Syngas-cool2 534 2 13.2 262.7 60.6 bar 13.2 kg/s 0 551 4 0.0 60.6 bar -0 0.0 kg/s 130 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 172 MW 97 MW 121 MW Output: Methanol DH Oxygen Syngas 205 MW 76 MW 0 MW 9 MW Energy content in DH water = 76 MW 0.17 120 C DH-cooler Steam 45.63 130 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 35 0 46 0.00 0.11 * for electrolyser Urenhed: 0.016 % Methanol loss in distillation [%] = 1.0 Methanol molar-% = 99.98 Water / 671 1.0 0.566 1.0 bar 0.93 Comp-syngas2 47.07 4.0 MW 17 SAND 4.039 13.2 266.4 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 26 2 26 3 34 3 34 0.01 0.08 0.01 0.08 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 76% (with power for electrolyser) 70% (with total power) 99% Methanol 2 1.0 kg/s 535 144.0 bar Syngas-cool2 533 Heat exchanger GASCOOL2 0.40 mio. kr/MW-transferred 2 3 0.01 0.00 120 C 2 13.2 kg/s Comp-syngas2 534 Compressor COMPRE_1 4.50 mio. kr/MW 18 24 0.05 Cond-steam-1 47.07 251 C Meoh-convert 601 Meoh converter MEOH_CONVERTER ##### mio. kr/(kmol/s-syngas) 295 384 0.89 Gas composition at specific nodes (mol-%) 46.69 10.3 231.1 set-M Preheater-sy 602 Heat exchanger GASCOOL4 0.40 mio. kr/MW-transferred 3 4 0.01 793 794 3.5 bar 10.3 kg/s 601 51.9 478.1 144.0 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 3 4 4 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 1.72 4 100 C 2 51.9 kg/s Comp-recirc 605 Compressor COMPRE_1 4.50 mio. kr/MW 1 1 0.00 Species Split-meoh1 177.7 39.2 879.7 Steam 0 682 4 88 235 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 262 0 341 0 0.79 0.00 1 3 H2 N2 45.98 0.25 0.00 57.70 61.87 44.20 23.87 25.43 27.98 30.00 0.00 0.00 0.18 1.56 2.13 2.27 2.50 2.68 791 3.5 bar 17.2 30.6 bar Cond-steam-2 685 Heat exchanger HEATSNK0 0.40 mio. kr/MW-transferred 13 16 0.04 4 CO 42.73 0.00 22.49 30.14 16.13 3.88 4.13 4.54 4.87 792 39.2 kg/s 17.58 17.2 kg/s DH-cooler 804 Heat exchanger HEATEX_1 0.40 mio. kr/MW-transferred 2 3 0.01 6 CO2 5.24 0.00 5.09 3.72 32.37 44.09 46.98 51.68 55.41 Heatsourc-DH 4 100 C Cond-steam-1 235 C Heatsourc-DH 806 Heat exchanger HEATSRC0 0.40 mio. kr/MW-transferred 16 21 0.05 7 H2O-G 5.21 0.00 14.17 3.68 1.65 2.30 1.39 0.42 0.01 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 0.048 811 10 40.1 239.2 1.0 bar 0.048 0.70 0 806 2 DH water 239.2 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 17.2 30.6 bar 31.9 Meoh-convert Methanol 1.00 SAND converter 89 311 Total several DISTILLATION_STAGE's 1559 2002 4.69 11 36 40 CH4 AR CH3OH 0.48 0.12 0.00 0.00 0.00 0.00 0.55 0.00 0.00 0.34 0.08 0.00 3.01 4.10 4.37 0.75 1.03 1.09 0.32 18.61 14.33 4.81 1.20 6.88 5.16 1.29 0.57 8.356 239.2 kg/s 90 C 1.958 239.2 kg/s 50 C 0.115 0.1 kg/s 235 C 0.025 0.1 kg/s 220 C 3.78 17.2 kg/s 220 C 602 51.9 462.6 139.0 bar 607 38.7 210.9 144.0 bar Input prices GG H2S NG_ref-cool Syngas-loop1 Syngas-meoh- Syngas-loop2 Syngas-3 Syngas-meoh Syngas-loop3 131 Heatsourc-DH 177.7 28.9 648.6 783 39.2 888.8 Heatsourc-DH 3.5 bar Cond-steam-1 Cond-steam-1 Convert-cool 2 89 51.9 kg/s 235 C 2 41 38.7 kg/s 225 C Input Electric power Price 324 kr/GJ Output cost Comparable fuel prices 781 3.5 bar 784 39.2 kg/s 17.0 17.47 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 28.9 kg/s 4 100 C 685 30.6 bar 8.1 Preheater-sy NG 93 kr/GJ Methanol 46.7 kr/s 202 kr/GJ 228 kr/GJ 4.53 kr/kg 3.6 kr/l Methanol (commercial) 142 kr/GJ 2.5 kr/l 2 100 C Dis_stage_17 2 17.0 kg/s 41 606 2 41 0.70 SAND 29 Biomass 32 kr/GJ Oxygen 0.2 kr/s 411 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 41 38.7 144.0 bar 48.6 392.4 DH water 0 kr/ton Syngas 2.2 kr/s 198 kr/GJ - kr/GJ 1.06 kr/kg - kr/l Crude oil 58 kr/GJ 2.2 kr/l Cond-steam-2 0.2 MW 19 0.90 208.5 38.7 kg/s 640 139.0 bar 84 12.96 3.3 66.71 Water 32 kr/ton DH water 0.7 kr/s 45 kr/GJ 9 kr/GJ 0.00 kr/kg - kr/l Ethanol 100 kr/GJ 2.4 kr/l 0 681 4 SAND 0.151 63 C 2 48.6 kg/s 621 139.0 bar CO2 114 kr/ton Water 0 kr/s - kr/GJ - kr/GJ - kr/kg - kr/l Distillation column 189 0.75 Feed 17.0 3.756 30.6 bar 17.0 kg/s 220 C Preheater-sy 76.24 173 C Condenser-1 7.3 631 3.3 kg/s 4 173 C Preheater-sy Nomenclature: Cond-steam-2 2.15 0.65 If methanol and DH share the plant costs Condenser-1 88.8 19.14 621 631 4 (methanol and DH are the only products from the plant) - 11 705 706 19 3.5 bar 2 2.15 705 706 4 3.5 bar 6 SAND 31 44.0 291.5 643 139.0 bar 2 44.0 kg/s 5 139.0 bar 98 4.6 kg/s 139 C and the DH cost is fixed corresponding to the DH price: Output Cost flow Cost Methanol 38.4 kr/s 166 kr/Gjex Electrical power Node nr Pressure Transferred heat [MW] 66 19.3 kg/s 12 3.6 kg/s Condenser 57.09 139 C Preheater-sy DH water 11.3 kr/s 150 kr/Gjen Mass flow 129 C 129 C SAND 33 Condenser Temperature Dis_stage_1 0.01 811 8 49.1 1.0 bar Reboil-meoh2 8.2 0.01 0.50 0 805 2 DH water 49.1 1.0 bar Mechanical power 10 11.45 20.1 57.25 1.714 49.1 kg/s 0.402 49.1 kg/s 2.145 3.6 10.28 707 3.5 bar Cond-steam-2 90 C 41.18 605 2 50 C 699 3.5 bar 0.25 708 20.1 kg/s SAND 393 Condenser 38.7 139.0 bar 2.0 10.97 Condenser 700 3.6 kg/s 4 129 C 208.4 38.7 kg/s 611 139.0 bar 94.0 13.75 3.2 69.56 2 129 C Water / Methanol Methanol molar-% = 7.35 0 693 694 1 3.5 bar 2 0.8 kg/s Dis_stage_1 4 9.301 695 696 16 3.5 bar 45 15.6 kg/s 2 31.7 9.339 0.66 9.339 705 706 16 3.5 bar 54 15.6 kg/s 4 45.85 625 635 11 3.5 bar 2 Methanol molar-% = 88.8 60 C Comp-recirc Methanol/ 4 2.0 kg/s 2.167 60 C Syngas Split-syngas 621 139.0 bar 631 3.2 kg/s 4 60 C Preheater-sy Reboil-meoh2 Heat Exergy efficiency [-] 64 C set-x-2 129 C Reboil-meoh1 129 C Reboil-meoh1 234 11.1 kg/s 101 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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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 167 and 168: 0 1 1 1 P 2 M type NOD* 2 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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9. - 10. - 11. - 12. - 13. - 14. -
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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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