Design og modellering af metanolanlæg til VEnzin-visionen Bilag

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 2.7 -0 0.0 0.006
4H 3 0 4Exergy destruction cost flow - based on specific cost of output 1 1.0 bar Electrolyser 423 3.0 bar 0.02 412 2
5EX 5 Component cost flow 2 2.7 kg/s 44.8 MW 201 2 0.0 kg/s 0.0 3.0 bar NG
6 EX_CH * Number of decimals Electrolyser 0.085 15 C SAND 44.77 0.00 850 C 0.175 0.0 kg/s
7 EX_PH SAND 301 Electrolyser
NG_reformer
656 C
8X
9 EX*M
10 EX_CH*M Comp-O2-1
DH water
0.515 803 4
129.3 1.0 bar
Electrolyser
14.8
1.9
0.80
0 802 2
129.3 1.0 bar DH water
0.92
Steam reformer
0.02
NG_reformer
O2 11 EX_PH*M 0.0 MW 1 1.275 129.3 kg/s 2.4 0.312 0.3 35.01 1.058 129.3 kg/s 0.0 0.002
12 C
13 C/EX
SAND 3E-05 54 C
Electro-cool
3
4
1.0 bar
2.4 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 0.168
403
2
3.0 bar
0.0 kg/s
0.0
0
Ash
0.6 0.492
83 1.0 bar
4 0.6 kg/s
14 C/M
O2 0.126 7 4 0.126
0.90
2.4 1.0 bar
0.312 2.4 kg/s
90 C
Comp-O2-1
0.126 5 2
2.4 1.0 bar
0.312 2.4 kg/s
90 C
Comp-O2-1
DH water
Gas
0.126 90 C
Electrolyser
0.0 -0
6 1.0 bar
4 0.0 kg/s
14.15 90 C
Electrolyser
H2 O2 2E-04 401 2
0.0 1.0 bar
4E-04 0.0 kg/s
90 C
SAND 4E-04
3E-04 402 4
0.92
3E-04 0.0 3.0 bar
8E-04 0.0 kg/s
231 C
431 3.0 bar
4 0.0 kg/s
0.02 950 C
NG_reformer
0.00 850 C
NG_reformer
0.0 0.02
441 3.0 bar
2 0.0 kg/s
0.002 950 C
Heatex-O2
Gasifier
304 0.0 MW
SAND
0 800 C
Gasifier
0.0
0.014
3.1
33 2
1.0 bar
Steam
32
17.0 21.92
1.0 bar
801
2
13.7 0.112
1.0 bar
13.7 kg/s
15
4
3.0 1.377
1.0 bar
3.0 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 0.048
3.0 bar
0.0 kg/s
0.0
0.00 0.95 Heatex-O2
SAND 11
4.007 3.1 kg/s Heatex-GG-st 4 17.0 kg/s 0 50 C 0 60 C 0.0 MW 322 14.15 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 5E-05 0.0 MW 7
Heatex-NG
0.89
11
Gasifier
12.9 282.2
11
17.8
257
Gasifier
10 GG2
0.13 0.78
1.0 bar 1.7
17.8 kg/s
800 C
11
17.8
255.8
11 2
1.0 bar
17.8 kg/s
754 C
Heatex-GG-st
0.07 0.98 11
21.8 17.8
243.3
12 2 0.00 0.74
1.0 bar 2.3
17.8 kg/s
130 C Heatex-GG-DH
11
17.8
242.8
13 2
1.0 bar
17.8 kg/s
60 C
1.00
Gas cleaner 10.6
14.8 242.2
14 1.0 bar
0.00
Heatsink
14.15
14.15 511 2
0.3 1.0 bar
35.01 0.3 kg/s
90 C
Heatsink-H2
0.019 503 4
0.0 7.5 bar
SAND 0.002
0.002 502 4 0.002 0.001 501 2
0.92
0.0 7.5 bar 0.0 1.0 bar
CO2
0.015 411 2
NG0.0
3.0 bar
0.171 0.0 kg/s
25 C
Heatex-NG
451
Heatex-NG
SAND
0.0 0.1
3.0 bar
0.0
13 0.02 0.89
0 434 Water 2
0.0 3.0 bar
82 1.0 bar Heatex-GG-O2
Heatex-GG-st
Heatex-GG-DH SAND 9 Cleaner
4 14.8 kg/s 0.162 0.0 kg/s 0.006 0.0 kg/s 0.005 0.0 kg/s 2 0.0 kg/s 4E-06 0.0 kg/s
2 12.9 kg/s 0.13 9 2 Heatex-GG-O2 17.0 9.643 0 21 4 10.6 60 C 213 C 182 C 15 C 0.01 950 C 79 C
7.72 120 C 2.4 1.0 bar SAND 5 31 1.0 bar 0.0 1.0 bar Cleaner 14.15 512 2 28.02 524 4 15.1 284.6 Mixer-CO2-NG
Comp-CO2 Comp-CO2
Heatex-H2O Pres-sep-3
Gasifier
H2O [mass-%] = 0.05
Dry-wood
1.271 2.4 kg/s
790 C
Gasifier
2 17.0 kg/s
0.049 120 C
Heatex-GG-st
2E-19 0.0 kg/s
60 C 521
Heatex-GG-DH 2
15.1 277
1.0 bar
15.1 kg/s
0.3
35.01
1.0 bar
0.3 kg/s
90 C
15.1
284.4
7.5 bar
15.1 kg/s
228 C
531
2
28.04
7.5 bar
15.1 kg/s
228 C
1E-04 422 2
Water 0.0 3.0 bar
2E-06 0.0 kg/s
0.0 Heatex-H2O
0.00 0.68 SAND 15
0 453 Water 4
Steam
811
13.7 0.479
1.0 bar
24.72 64 C
Comp-GG-H2-1
Comp-GG-H2-1
5.8 MW 11
Mixer-GG-H2 Comp-GG-H2-2
57.1 33.33
Syngas-cool1
23 C
Heatex-H2O
0.0
7E-06
3.0 bar
0.0 kg/s
4 13.7 kg/s 0.92
SAND 5.817 571 1.0 bar Syngas-cool1 Comp-NG_ref 79 C
0.00 90 C 26.79 57.0 32.29 6 57.1 kg/s SAND 21 0.0 MW 5 0.0 Heatex-H2O
0.0 0.044 0.0
13.9 17.91 Heatex-GG-DH
15.1 282.4 563 1.0 bar 0.17 150 C 3.4 SAND 0.003 0.0 0.092 0.0 0.044 0.0 0.019
0.63
219.1
Steam_dryer Biomass (dry)
SAND 1
35 4 0.52 32.9 0.63 34 2
1.0 bar Steam dryer 7.72 207.5 1.0 bar
34 1.0 bar
4 13.9 kg/s
0.061 730 C
Split-steam2
522 3.7 bar
2 15.1 kg/s
26.79 228 C
Cooler-GG-H2
2 57.0 kg/s
0.16 120 C
Cooler-GG-H2
3.4
0.17 0.81
26.79 523 2
15.1 3.7 bar
0.92
28.02
Syngas-cool1
561
2
0.163
57.1 32.32
1.0 bar
57.1 kg/s
120 C
0.17 0.81
0 541 4
0.0 7.5 bar
3E-18 0.0 kg/s
130 C
Water
Reformat
0.017 462 2 0.017
0.0 7.5 bar
0.157 0.0 kg/s
0.016 461 2
0.92
0.0 3.0 bar
0.154 0.0 kg/s
452 3.0 bar
2 0.0 kg/s
0.01 79 C
Mixer-NG_ref
433 3.0 bar
2 0.0 kg/s
0.005 79 C
Mixer-NG_ref
442 3.0 bar
2 0.0 kg/s
0.002 303 C
Mixer-NG_ref
124.1 219.1 kg/s 128.5 207.5 kg/s Cooler-GG-H2 57.0 33.29 281.2 15.1 kg/s Syngas-cool1 15.1 283.3 Syngas-cool1
226 C 108 C
120 C 24.6 283.1 200 C SAND 19 571 1.0 bar 130 C Comp-GG-H2-2 532 7.5 bar
Mixer-CO2-NG
Comp-NG_ref
Steam_dryer
81 1.0 bar Steam_dryer
4 57.0 kg/s Comp-GG-H2-2 2 15.1 kg/s
2
7.577
24.6 kg/s
15 C
Steam
0.17 150 C
Cooler-GG-H2
3.5 MW
SAND
13
3.49
28.04 130 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)
8.5 4.827
41 1.0 bar
2 8.5 kg/s
Steam
0.92
29.28
15.1 286.5
533 15.2 bar
4 15.1 kg/s
Syngas 29.28 228 C
3.5 MW
SAND
15
3.493
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]
68
0
0
Total
price
[mio. kr]
88
0
0
C
[kr/s]
0.20
0.00
0.00
Input:
NG
Biomass
Power*
Total power
* for electrolyser
0 MW
283 MW
45 MW
65 MW
Output:
Methanol
DH
Oxygen
Syngas
231 MW
11 MW
0 MW
35 MW
SAND 79 0.024 120 C 1.0 0.59 set_temp-2
Gasifier
9 Gasifier
GASIFI_3 3.80 mio. kr/MW-biomass 900 1170 2.71
DH-condenser
0.72 19.8 0.56 811 12
DH condenser0.56
129.3 1.0 bar
581
2
0.00
1.0 bar
1.0 kg/s
159 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
9
1
1
11
1
0.00
0.03
0.00
Methanol-efficiency 1:
Methanol-efficiency 2:
Total efficiency:
70% (with power for electrolyser)
66% (with total power)
80%
8.5 0.336 4.516 129.3 kg/s DH-cooler DH-cooler
57.1 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 33.33 57.1 kg/s Steam_dryer
34 Steam dryer DRYER_04 4.10 mio. kr/(kg/s)-evaporated 48 62 0.14
4 8.5 kg/s
0 95 C
DH-condenser
DH-condenser
428.0 14.95
811 1.0 bar
0.000 811 6
0.5 1.0 bar
0.016 0.5 kg/s
0.53 0.1 0 804 2
DH cooler
DH water
0.00 0.5 1.0 bar
0.004 0.5 kg/s 23.4 14.99
0.163 562 2
57.1 1.0 bar
150 C
Syngas-cool2 3.4
0.17 0.81
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
8
0
0
10
0
0
0.02
0.00
0.00 Energy
Water
2 428.0 kg/s
0.62 90 C
DH
DH water
90 C
DH-cooler
35
6
1.0 0.566
1.0 bar
1.0 kg/s
50 C
DH-cooler
571 1.0 bar
10 23.4 kg/s
0.07 225 C
Cond-steam-1
32.32 57.1 kg/s
120 C
Syngas-cool2
534
2
15.1 285.3
15.2 bar
15.1 kg/s
0 551 4
0.0 15.2 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
237 MW
45 MW
65 MW
Output:
Methanol
DH
Oxygen
Syngas
205 MW
72 MW
0 MW
33 MW
Energy content in DH water = 72 MW 0.00 120 C
DH-cooler
Steam
29.28 130 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
26
0
34
0.00
0.08
* for electrolyser
Urenhed:
0.026 %
Methanol loss in distillation [%] = 1.0
Methanol molar-% = 99.97
Water /
671
23.4 13.28
1.0 bar
0.93
Comp-syngas2
31.04 5.0 MW 17
SAND 4.957
15.1 289.9
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
16
1
16
2
20
2
20
0.00
0.05
0.00
0.05
Methanol-efficiency 1:
Methanol-efficiency 2:
Total efficiency:
73% (with power for electrolyser)
68% (with total power)
103%
Methanol
2 23.4 kg/s 535 40.0 bar Syngas-cool2 533 Heat exchanger GASCOOL2 0.40 mio. kr/MW-transferred 1 2 0.00
0.06 120 C 2 15.1 kg/s Comp-syngas2
534 Compressor COMPRE_1 4.50 mio. kr/MW 22 29 0.07
Cond-steam-1
31.04 269 C Meoh-convert
601 Meoh converter MEOH_CONVERTER ##### mio. kr/(kmol/s-syngas) 550 715 1.65 Gas composition at specific nodes (mol-%)
29.63 10.3 231.1 set-M
Preheater-sy 602 Heat exchanger GASCOOL4 0.40 mio. kr/MW-transferred 7 9 0.02
793
794
3.5 bar
10.3 kg/s 601
101.6 969.3
40.0 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
0
8
0
10
0.00
0.02
Node 10
3
15 431 534 601 602 640 643 605
15 23 33 35 41 43 39 37
M-factor
1.47
4 100 C 2 101.6 kg/s Comp-recirc
605 Compressor COMPRE_1 4.50 mio. kr/MW 6 8 0.02
Species
Split-meoh1
80.83 28.1 630.4 Steam
0 682 4
115 235 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
249
2
324
3
0.75
0.01
1
3
H2
N2
46.08
0.24
0.00 57.09 55.57 36.59 27.41 27.41 27.41 30.00
0.00 0.00 0.22 1.16 1.36 1.36 1.36 1.48
791 3.5 bar 18.7 30.6 bar Cond-steam-2
685 Heat exchanger HEATSNK0 0.40 mio. kr/MW-transferred 12 16 0.04 4 CO 40.49 0.00 22.34 37.67 30.98 26.18 26.18 26.18 28.65
792 28.1 kg/s 19.14 18.7 kg/s DH-cooler
804 Heat exchanger HEATEX_1 0.40 mio. kr/MW-transferred 0 0 0.00 6 CO2 6.19 99.94 4.97 0.02 25.64 31.56 31.56 31.56 34.54
Heatsourc-DH 4 100 C Cond-steam-1 235 C Heatsourc-DH
806 Heat exchanger HEATSRC0 0.40 mio. kr/MW-transferred 11 15 0.03 7 H2O-G 6.51 0.00 15.55 6.07 1.58 0.28 0.28 0.28 0.03
SAND 390 Cond-meoh SAND 35 Convert-cool * The distillation column is composed of 9 H2S 0.00 0.06 0.00 0.00 0.00 0.00 0.00 0.00 0.00
0.035 811 10 28.7
171.4 1.0 bar 0.035 0.70
0 806 2
DH water
171.4 1.0 bar
0 683 2
2.6 30.6 bar
4.9
0.07 0.81
0 684 4
2.6 30.6 bar
Water
0 681 2
18.7 30.6 bar
34.7 Meoh-convert
Methanol 1.00 SAND
converter 116
311
Total several DISTILLATION_STAGE's 1963 2537 5.91 11
36
40
CH4
AR
CH3OH
0.36
0.12
0.00
0.00
0.00
0.00
0.05
0.00
0.00
0.34
0.11
0.00
1.75 2.05 2.05 2.05
0.56 0.65 0.65 0.65
1.74 10.51 10.51 10.51
2.24
0.71
2.35
5.989 171.4 kg/s
90 C
1.404 171.4 kg/s
50 C
2.691 2.6 kg/s
235 C
0.579 2.6 kg/s
220 C
4.116 18.7 kg/s
220 C 602
101.6 952.6
35.0 bar 607
86.4 679.7
40.0 bar Input prices
GG
H2S
NG_ref-cool Syngas-loop1 Syngas-meoh- Syngas-loop2
Syngas-3 Syngas-meoh Syngas-loop3
51.2
Heatsourc-DH 80.83
17.8 399.3 783
28.1 637 Heatsourc-DH
3.5 bar
Cond-steam-1 Cond-steam-1 Convert-cool
2 101.6 kg/s
116 235 C
2
84
86.4 kg/s
225 C
Input
Electric power
Price
324 kr/GJ Output cost
Comparable fuel prices
781 3.5 bar 784 28.1 kg/s 16.1 16.45 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 17.8 kg/s 4 100 C 685 30.6 bar 17.7 Preheater-sy NG 93 kr/GJ Methanol 29.6 kr/s 128 kr/GJ 145 kr/GJ 2.88 kr/kg 2.3 kr/l Methanol (commercial) 142 kr/GJ 2.5 kr/l
2 100 C Dis_stage_17 2 16.1 kg/s 84 606 2 84 0.89 SAND 29 Biomass 32 kr/GJ Oxygen 0.0 kr/s 404 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 84 86.4 40.0 bar 101.6 946.4 DH water 0 kr/ton Syngas 4.4 kr/s 124 kr/GJ - kr/GJ 0.96 kr/kg - kr/l Crude oil 58 kr/GJ 2.2 kr/l
Cond-steam-2 1.4 MW 19 0.90 674.2 86.4 kg/s 640 35.0 bar 1 2E-28 0.0 2E-27 Water 32 kr/ton DH water 0.6 kr/s 42 kr/GJ 9 kr/GJ 0.00 kr/kg - kr/l Ethanol 100 kr/GJ 2.4 kr/l
0 681 4 SAND 1.437 73 C 2 101.6 kg/s 621 35.0 bar CO2 114 kr/ton Water 0 kr/s - kr/GJ - kr/GJ - kr/kg - kr/l
Distillation
column
99 0.80
Feed
16.1
3.537
30.6 bar
16.1 kg/s
220 C
Preheater-sy 116.4 110 C
Condenser-1
0.1
631 0.0 kg/s
4 110 C
Preheater-sy
Nomenclature:
Cond-steam-2 0.08 1.06 If methanol and DH share the plant costs
Condenser-1 0.0 -0 621 631 4 (methanol and DH are the only products from the plant) -
18 705 706
17 3.5 bar
2 0.08 705 706
0 3.5 bar
6
SAND 31 101.6 946.3
643 35.0 bar
2 101.6 kg/s
0
0
35.0 bar
0.0 kg/s
109 C
and the DH cost is fixed corresponding to the DH price:
Output Cost flow Cost
Methanol 23.8 kr/s 103 kr/Gjex Electrical power
Node nr
Pressure
Transferred heat [MW]
151 17.1 kg/s 1 0.0 kg/s Condenser 116.4 109 C Preheater-sy
DH water 10.8 kr/s 150 kr/Gjen Mass flow
118 C 118 C SAND 33 Condenser
Temperature
Dis_stage_1 0.02 811 8
113.1 1.0 bar
Reboil-meoh2 19.0
0.02 0.64
0 805 2
DH water
113.1 1.0 bar Mechanical power
10
18.44 17.4 145.3 3.951 113.1 kg/s 0.926 113.1 kg/s 0.084 0.1 0.652
707 3.5 bar Cond-steam-2 90 C 83.21 605 2 50 C 699 3.5 bar 0.25
708 17.4 kg/s SAND 393 Condenser
86.4 35.0 bar 4.5 35.41 Condenser
700 0.0 kg/s
4 118 C 672.9 86.4 kg/s 611 35.0 bar 97.0 28.85 10.6 233.3 2 118 C
Water /
Methanol
Methanol molar-% = 24.82
0 693 694
0 3.5 bar
2 0.3 kg/s
Dis_stage_1
4 18.35 695 696
17 3.5 bar
142 17.0 kg/s
2 29.9
18.39 0.61
18.39 705 706
17 3.5 bar
150 17.0 kg/s
4
28.85 625 635
11 3.5 bar
2
Methanol molar-% = 97.0
60 C
Comp-recirc
Methanol/
4 4.5 kg/s
4.379 60 C
Syngas Split-syngas
621 35.0 bar
631 10.6 kg/s
4 60 C
Preheater-sy
Reboil-meoh2
Heat
Exergy efficiency [-]
64 C
set-x-2
118 C
Reboil-meoh1
118 C
Reboil-meoh1
233 10.6 kg/s
61 C
meas_flow
Methanol mass flow = 10.4 kg/s
water