Design og modellering af metanolanlæg til VEnzin-visionen Bilag

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26. Flowsheets for metanolanlæg – for parametervariationen (brint/kulstof-forholdet i syngassen) Flowsheets for brint/kulstof-forhold på M=1,55 og M=2,35. Sorteret efter brint/kulstof-forhold – anlægget på M=1,55 først.
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 41.0 MW 201 2 0.0 kg/s 0.0 10.0 bar NG 6 EX_CH * Number of decimals Electrolyser 0.078 15 C SAND 41 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 0.45 803 4 111.3 1.0 bar Electrolyser 13.55 1.7 0.80 0 802 2 111.3 1.0 bar DH water 0.93 Steam reformer 0.02 NG_reformer O2 11 EX_PH*M 0.0 MW 1 1.11 111.3 kg/s 2.2 0.286 0.3 32.06 0.912 111.3 kg/s 0.0 0.002 12 C 13 C/EX SAND 2E-05 54 C Electro-cool 3 4 1.0 bar 2.2 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 0.452 83 1.0 bar 4 0.6 kg/s 14 C/M O2 0.116 7 4 0.116 0.90 2.2 1.0 bar 0.286 2.2 kg/s 90 C Comp-O2-1 0.116 5 2 2.2 1.0 bar 0.286 2.2 kg/s 90 C Comp-O2-1 DH water Gas 0.116 90 C Electrolyser 0.0 -0 6 1.0 bar 4 0.0 kg/s 12.99 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 0.019 3.4 33 2 1.0 bar Steam 32 16.3 21.02 1.0 bar 801 2 13.1 0.107 1.0 bar 13.1 kg/s 15 4 3.2 1.501 1.0 bar 3.2 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 4.384 3.4 kg/s Heatex-GG-st 4 16.3 kg/s 0 50 C 0 60 C 0.0 MW 322 12.99 0.0 MW 9 Comp-CO2 0.005 950 C 730 C SAND 7 0.09 730 C Heatex-GG-DH Cleaner SAND 0.0 SAND 5E-05 0.0 MW 7 Heatex-NG 0.89 10 Gasifier 11.9 259.5 10 16.9 236.9 Gasifier 10 GG2 0.12 0.78 1.0 bar 1.6 16.9 kg/s 800 C 10 16.9 235.7 11 2 1.0 bar 16.9 kg/s 756 C Heatex-GG-st 0.09 0.98 10 20.9 16.9 223.8 12 2 0.00 0.74 1.0 bar 2.2 16.9 kg/s 130 C Heatex-GG-DH 10 16.9 223.3 13 2 1.0 bar 16.9 kg/s 60 C 1.00 Gas cleaner 9.7 13.6 222.6 14 1.0 bar 0.00 Heatsink 12.99 12.99 511 2 0.3 1.0 bar 32.06 0.3 kg/s 90 C Heatsink-H2 0.019 503 4 0.0 19.1 bar SAND 0.003 0.002 502 4 0.002 0.001 501 2 0.93 0.0 19.1 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 11.9 kg/s 0.12 9 2 Heatex-GG-O2 16.3 9.249 0 21 4 9.7 60 C 254 C 275 C 15 C 0.01 950 C 107 C 7.10 120 C 2.2 1.0 bar SAND 5 31 1.0 bar 0.0 1.0 bar Cleaner 12.99 512 2 27.6 524 4 13.9 265.2 Mixer-CO2-NG Comp-CO2 Comp-CO2 Heatex-H2O Pres-sep-3 Gasifier H2O [mass-%] = 0.05 Dry-wood 1.164 2.2 kg/s 790 C Gasifier 2 16.3 kg/s 0.064 120 C Heatex-GG-st 2E-18 0.0 kg/s 60 C 521 Heatex-GG-DH 2 13.9 254.5 1.0 bar 13.9 kg/s 0.3 32.06 1.0 bar 0.3 kg/s 90 C 13.9 265 19.1 bar 13.9 kg/s 304 C 531 2 27.62 19.1 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 13.1 0.457 1.0 bar 22.71 64 C Comp-GG-H2-1 Comp-GG-H2-1 8.0 MW 11 Mixer-GG-H2 Comp-GG-H2-2 35.8 22.16 Syngas-cool1 33 C Heatex-H2O 0.0 2E-05 10.0 bar 0.0 kg/s 4 13.1 kg/s 0.93 SAND 7.98 571 1.0 bar Syngas-cool1 Comp-NG_ref 109 C 0.00 90 C 25.54 35.7 20.25 6 35.8 kg/s SAND 21 0.0 MW 5 0.0 Heatex-H2O 0.0 0.046 0.0 12.9 16.64 Heatex-GG-DH 13.9 261.9 563 1.0 bar 0.15 200 C 5.7 SAND 0.002 0.0 0.094 0.0 0.046 0.0 0.018 0.42 109.6 Steam_dryer Biomass (dry) SAND 1 35 4 0.45 30.3 0.42 34 2 1.0 bar Steam dryer 7.10 98.9 1.0 bar 34 1.0 bar 4 12.9 kg/s 0.071 730 C Split-steam2 522 5.9 bar 2 13.9 kg/s 25.54 304 C Cooler-GG-H2 2 35.7 kg/s 0.14 120 C Cooler-GG-H2 5.7 0.15 0.82 25.54 523 2 13.9 5.9 bar 0.93 27.6 Syngas-cool1 561 2 0.14 35.8 20.27 1.0 bar 35.8 kg/s 120 C 0.15 0.82 0 541 4 0.0 19.1 bar -0 0.0 kg/s 130 C Water Reformat 0.017 462 2 0.017 0.0 19.1 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 62.07 109.6 kg/s 67.55 98.9 kg/s Cooler-GG-H2 35.7 22.13 259.6 13.9 kg/s Syngas-cool1 13.9 262.9 Syngas-cool1 245 C 154 C 120 C 22.6 260.4 274 C SAND 19 571 1.0 bar 130 C Comp-GG-H2-2 532 19.1 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 13.9 kg/s 2 6.968 22.6 kg/s 15 C Steam 0.15 200 C Cooler-GG-H2 5.8 MW SAND 13 5.796 27.62 130 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) 7.3 4.131 41 1.0 bar 2 7.3 kg/s Steam 0.93 29.67 13.9 268.3 533 62.0 bar 4 13.9 kg/s Syngas 29.67 304 C 5.8 MW SAND 15 5.8 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] 62 0 0 Total price [mio. kr] 81 0 0 C [kr/s] 0.19 0.00 0.00 Input: NG Biomass Power* Total power * for electrolyser 0 MW 260 MW 41 MW 66 MW Output: Methanol DH Oxygen Syngas 231 MW 12 MW 0 MW 13 MW SAND 79 0.029 120 C 28.6 17.72 set_temp-2 Gasifier 9 Gasifier GASIFI_3 3.80 mio. kr/MW-biomass 827 1076 2.49 DH-condenser 0.72 16.9 0.50 811 12 DH condenser0.50 111.3 1.0 bar 581 2 0.12 1.0 bar 28.6 kg/s 200 C Steam 0.17 571 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 8 1 1 11 1 0.00 0.03 0.00 Methanol-efficiency 1: Methanol-efficiency 2: Total efficiency: 77% (with power for electrolyser) 71% (with total power) 78% 7.3 0.287 3.889 111.3 kg/s DH-cooler DH-cooler 42.1 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 26.04 42.1 kg/s Steam_dryer 34 Steam dryer DRYER_04 4.10 mio. kr/(kg/s)-evaporated 44 57 0.13 4 7.3 kg/s 0 95 C DH-condenser DH-condenser 443.8 15.5 811 1.0 bar 0.006 811 6 27.2 1.0 bar 0.95 27.2 kg/s 0.48 4.6 0 804 2 DH cooler DH water 0.01 27.2 1.0 bar 0.223 27.2 kg/s 1.0 0.639 0.165 562 2 42.1 1.0 bar 200 C Syngas-cool2 6.7 0.17 0.86 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 7 0 0 9 0 0 0.02 0.00 0.00 Energy Water 2 443.8 kg/s 0.57 90 C DH DH water 90 C DH-cooler 35 6 28.6 16.21 1.0 bar 28.6 kg/s 50 C DH-cooler 571 1.0 bar 10 1.0 kg/s 0.00 225 C Cond-steam-1 23.82 42.1 kg/s 120 C Syngas-cool2 534 2 13.4 265.6 62.0 bar 13.4 kg/s 0 551 4 0.5 62.0 bar 0.046 0.5 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 218 MW 41 MW 66 MW Output: Methanol DH Oxygen Syngas 205 MW 75 MW 0 MW 11 MW Energy content in DH water = 75 MW 0.12 120 C DH-cooler Steam 29.67 135 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 36 0 47 0.00 0.11 * for electrolyser Urenhed: 0.003 % Methanol loss in distillation [%] = 1.0 Methanol molar-% = ##### Water / 671 1.0 0.566 1.0 bar 0.93 Comp-syngas2 31.05 3.9 MW 17 SAND 3.891 13.4 269.2 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: 79% (with power for electrolyser) 72% (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 3 3 0.01 0.00 120 C 2 13.4 kg/s Comp-syngas2 534 Compressor COMPRE_1 4.50 mio. kr/MW 18 23 0.05 Cond-steam-1 31.05 255 C Meoh-convert 601 Meoh converter MEOH_CONVERTER ##### mio. kr/(kmol/s-syngas) 328 427 0.99 Gas composition at specific nodes (mol-%) 31.24 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 69.0 513.8 144.0 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 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 1.55 4 100 C 2 69.0 kg/s Comp-recirc 605 Compressor COMPRE_1 4.50 mio. kr/MW 1 1 0.00 Species Split-meoh1 125.1 41.2 925.5 Steam 0 682 4 63 235 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 247 0 320 0 0.74 0.00 1 3 H2 N2 46.08 0.23 0.00 57.70 57.39 29.76 0.00 0.00 0.23 1.78 9.95 10.49 11.34 11.84 2.35 2.47 2.68 2.79 791 3.5 bar 18.2 30.6 bar Cond-steam-2 685 Heat exchanger HEATSNK0 0.40 mio. kr/MW-transferred 13 18 0.04 4 CO 38.18 0.00 22.49 36.99 28.62 19.50 20.55 22.23 23.20 792 41.2 kg/s 18.68 18.2 kg/s DH-cooler 804 Heat exchanger HEATEX_1 0.40 mio. kr/MW-transferred 2 2 0.01 6 CO2 7.14 99.95 5.09 0.02 34.50 47.77 50.34 54.45 56.85 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 7.96 0.00 14.17 4.99 1.96 0.21 0.12 0.03 0.00 SAND 390 Cond-meoh SAND 35 Convert-cool * The distillation column is composed of 9 H2S 0.00 0.05 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.051 811 10 42.2 251.6 1.0 bar 0.051 0.70 0 806 2 DH water 251.6 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 18.2 30.6 bar 33.9 Meoh-convert Methanol 1.00 SAND converter 64 311 Total several DISTILLATION_STAGE's 1681 2161 5.06 11 36 40 CH4 AR CH3OH 0.28 0.11 0.00 0.00 0.00 0.00 0.55 0.00 0.00 0.27 0.11 0.00 2.15 2.82 2.98 0.86 1.13 1.19 0.37 16.27 11.87 3.22 1.29 4.77 3.36 1.34 0.61 8.789 251.6 kg/s 90 C 2.06 251.6 kg/s 50 C 0.115 0.1 kg/s 235 C 0.025 0.1 kg/s 220 C 4.017 18.2 kg/s 220 C 602 69.0 497.4 139.0 bar 607 55.6 244.4 144.0 bar Input prices GG H2S NG_ref-cool Syngas-loop1 Syngas-meoh- Syngas-loop2 Syngas-3 Syngas-meoh Syngas-loop3 93.87 Heatsourc-DH 125.1 30.9 694.4 783 41.2 935.1 Heatsourc-DH 3.5 bar Cond-steam-1 Cond-steam-1 Convert-cool 2 64 69.0 kg/s 235 C 2 32 55.6 kg/s 225 C Input Electric power Price 324 kr/GJ Output cost Comparable fuel prices 781 3.5 bar 784 41.2 kg/s 18.1 18.57 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 30.9 kg/s 4 100 C 685 30.6 bar 9.8 Preheater-sy NG 93 kr/GJ Methanol 31.2 kr/s 135 kr/GJ 152 kr/GJ 3.03 kr/kg 2.4 kr/l Methanol (commercial) 142 kr/GJ 2.5 kr/l 2 100 C Dis_stage_17 2 18.1 kg/s 32 606 2 32 0.70 SAND 29 Biomass 32 kr/GJ Oxygen 0.0 kr/s 405 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 32 55.6 144.0 bar 65.7 418.8 DH water 0 kr/ton Syngas 1.7 kr/s 131 kr/GJ - kr/GJ 0.57 kr/kg - kr/l Crude oil 58 kr/GJ 2.2 kr/l Cond-steam-2 0.2 MW 19 0.90 241.4 55.6 kg/s 640 139.0 bar 98 9.615 3.3 74.35 Water 32 kr/ton DH water 0.6 kr/s 36 kr/GJ 8 kr/GJ 0.00 kr/kg - kr/l Ethanol 100 kr/GJ 2.4 kr/l 0 681 4 SAND 0.183 63 C 2 65.7 kg/s 621 139.0 bar CO2 114 kr/ton Water 0 kr/s - kr/GJ - kr/GJ - kr/kg - kr/l Distillation column 173 0.88 Feed 18.1 3.992 30.6 bar 18.1 kg/s 220 C Preheater-sy 54.16 158 C Condenser-1 7.7 631 3.3 kg/s 4 158 C Preheater-sy Nomenclature: Cond-steam-2 8.90 0.58 If methanol and DH share the plant costs Condenser-1 98.8 13.7 621 631 4 (methanol and DH are the only products from the plant) - 48 705 706 27 3.5 bar 2 8.90 705 706 5 3.5 bar 6 SAND 31 61.0 310.4 643 139.0 bar 2 61.0 kg/s 5 139.0 bar 105 4.7 kg/s 122 C and the DH cost is fixed corresponding to the DH price: Output Cost flow Cost Methanol 22.3 kr/s 96.4 kr/Gjex Electrical power Node nr Pressure Transferred heat [MW] 366 27.4 kg/s 68 5.0 kg/s Condenser 40.46 122 C Preheater-sy DH water 11.2 kr/s 150 kr/Gjen Mass flow 112 C 112 C SAND 33 Condenser Temperature Dis_stage_1 0.01 811 8 40.6 1.0 bar Reboil-meoh2 6.8 0.01 0.54 0 805 2 DH water 40.6 1.0 bar Mechanical power 10 47.86 27.5 357.7 1.419 40.6 kg/s 0.332 40.6 kg/s 8.895 5.1 66.05 707 3.5 bar Cond-steam-2 90 C 31.66 605 2 50 C 699 3.5 bar 0.25 708 27.5 kg/s SAND 393 Condenser 55.6 139.0 bar 2.9 12.7 Condenser 700 5.0 kg/s 4 112 C 241.3 55.6 kg/s 611 139.0 bar 99.3 7.137 2.4 54.4 2 112 C Water / Methanol Methanol molar-% = 43.46 0 693 694 0 3.5 bar 2 0.2 kg/s Dis_stage_1 4 38.96 695 696 22 3.5 bar 289 22.3 kg/s 2 33.7 39.01 0.58 39.01 705 706 22 3.5 bar 298 22.3 kg/s 4 30.45 625 635 10 3.5 bar 2 Methanol molar-% = 98.7 60 C Comp-recirc Methanol/ 4 2.9 kg/s 1.666 60 C Syngas Split-syngas 621 139.0 bar 631 2.4 kg/s 4 60 C Preheater-sy Reboil-meoh2 Heat Exergy efficiency [-] 64 C set-x-2 112 C Reboil-meoh1 112 C Reboil-meoh1 234 10.5 kg/s 100 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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14. Metanolproduktion, NZIC New Zea
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Maui Gas Supply Kapuni Gas Supply N
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Page 143 and 144: The reaction of the synthesis gas c
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Page 149 and 150: NYKOMB SYNERGETICS 2. Methanol Plan
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Page 155 and 156: 16. Metanolproduktion, Wikipedia Wi
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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 241 and 242:
17.126.4 Conditions ˙m1 > 0 ˙m2 <
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 249 and 250:
17.129.4 Conditions ˙m1 > 0 ˙m2 <
Page 251 and 252:
17.130.4 Conditions ˙m1 > 0 ˙m2 <
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 265 and 266:
17.138.4 Conditions ˙m1 > 0 ˙m2 <
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 331 and 332:
Page 333 and 334:
VEnzin.for c:/dna/source/ RES(1) =
Page 335 and 336:
Page 337 and 338:
Page 339 and 340:
35. Metanol (fluid) til DNA - Fortr
Page 341 and 342:
methanol.for d:/DTU/Eksamensprojekt
Page 343 and 344:
Page 345 and 346:
Page 347 and 348:
Page 349 and 350:
Page 351 and 352:
Page 353 and 354:
Page 355 and 356:
Page 357 and 358:
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Design og modellering af metanolanlæg til VEnzin-visionen Bilag

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