7/29/2019 SK_052_B.doc

1/8

MATERIAL BALANCE

A. COAL GASIFICATION

Mass Flow

(MT/day)

Wet

CoalWater P-1 Oxygen P-2 Slag Syngas

Coal 1280.00 0.00 0.00 0.00 0.00 0.00 0.00

H2O 0.00549.0

0683.40 0.00 34.56 0.00 34.56

N2 0.00 0.00 17.02 0.00 24.38 0.00 24.38O2 0.00 0.00 149.38 900.00 0.00 0.00 0.00

S 0.00 0.00 14.08 0.00 0.00 0.00 0.00

H2 0.00 0.00 56.06 0.00 96.42 0.00 96.42

C 0.00 0.00 765.70 0.00 0.00 0.00 0.00

ASH 0.00 0.00 143.36 0.00 143.36 143.36 0.00

CO 0.00 0.00 0.00 0.002135.8

10.00 2135.81

CO2 0.00 0.00 0.00 0.00 45.79 0.00 45.79

H2S 0.00 0.00 0.00 0.00 21.25 0.00 21.25

Total (MT/Day) 1280.00549.0

0

1829.0

0 900.002501.5

8 143.36 2358.22

7/29/2019 SK_052_B.doc

2/8

Pressure (Mpa) 0.101 0.101 4.17 0.101 5.17 5.16 5.16

Temperature 25 25 25 25 1315 711 711

B. ACID GAS REMOVAL

2 32CO H CH OH + (Eqn. 1)

2 2 2CO H CO H O+ + (Eqn. 2)

2 2 3 23CO H CH OH H O+ + (Eqn. 3)

7/29/2019 SK_052_B.doc

3/8

C. WATER GAS SHIFT PROCESS

Mass F

low (M

T/hr)

P1 P2 P3 P4 P5 P6 P7 P8 P9

Mass Flow

(MT/hr)P1 P2 P3 P4 P5 P6 P7 P8 P9 P10

H2O 1.44 1.44 0 0 0 0.15 0.15 0.15 00.21

4

N2 1.016 1.016 0 0 0 0 0 0 0 0

S 0 0 0 0 0 0 0 00.55

40

SO2 0 0 0 0 0 0 0 0.37 0 0

H2 4.018 4.018 0 0 0 0 0 0 0 0

CO88.99

2

88.99

20 0 0 0 0 0 0 0

CO2 1.908 1.908 0 0 0 0 0 0 0 0

H2S 0.886 0.8860.88

6

0.88

6

0.88

6

0.60

4

0.60

4

0.60

40 0

Total

(MT/Day)98.26 98.26

0.88

6

0.88

6

0.88

6

0.75

4

0.75

4

1.12

4

0.55

4

0.21

4Pressure

(Mpa)6.27 6.27 6.27 2.41 2.41 2.41 2.41 2.41 2.41 2.41

Temperature 467 39.8 4626.8

51000 1000 350 350 300 300

7/29/2019 SK_052_B.doc

4/8

H2O 1.44 1.44 1.44 0.000346 0.000346 0.166 0.166 0.166 0

N2 1.016 1.016 1.016 1.014 1.014 1.014 1.014 0 1.014

H2 4.018 4.018 4.018 5.124 4.924 6.956 6.956 0 48.16

CO 89 89 72.72 76.406 76.406 48.16 48.16 0 66.0822

CO2 1.908 1.908 1.908 21.7 21.7 66.082 66.082 0 66.0822

Total

(MT/D

ay)

97.38

2

97.38

2

97.38

2104.044 104.044

122.37

8

122.37

80.166 122.212

Pressur

e

(Mpa)

6.27 5.17 5.17 5.17 5.17 5.17 5.17 5.17 5.17

Temper

ature46 38.15 371 354 200 184 150 150 150

D. METHANOL SYNTHESIS

PFR

1

PFR

2

PFR

3

PFR

4

PFR

5

IN OUT IN OUT IN OUT IN OUT IN OUT

7/29/2019 SK_052_B.doc

5/8

Flow

(MT/day)

CO 115.6Trac

e231.2

101.

8217.4

Trac

e

462.

4340.4 360 12.2

CO2 158.6

156.

2 473.4

437.

8 596.6 576

120

9.6 432.4 750 228.4H2O 0.4 1.4 2.2 16.6 17 25.4 27 345.4 346.2 559.4

H2 16.8Trac

e33.4 10 26.6

Trac

e66.8 Trace 33.4 Trace

CH4O 0 227 227405.

4405.4 740 740 987.8 987.8

1063.

2

Temp (K) 663 1744 798 945 762 815 500 556 522 571

E. METHANOL REFINING

Distillatio

n1

Distillati

on2

Distillati

on3

Distillati

on4

Flow

(Ton/day

)

InDistilla

teIn

Distill

ateIn

Distill

ateIn

Distill

ate

Methano 1063 1060.2 1060.2 1059. 1059.8 1059 1059 1058.

7/29/2019 SK_052_B.doc

6/8

l 8 4

Ethanol 15.2 3.868 3.868 0.708 0.708 0.156 0.156 0

Water 558 Trace Trace Trace Trace Trace Trace Trace

ENERGY BALANCE

Gasifier

As coal, or any other carbonaceous feedstock enters a gasifier, its

temperature increases and

any moisture present in the material quickly escapes to the gas phase.

Pyrolysis (also known as devolatilization) occurs as the feedstock

temperature continues to increase. During pyrolysis, the feedstock

undergoes heat-induced decomposition, which results in the liberation of

volatile constituents to the gas phase. Volatile matter can include: H2,

CO2, CO, CH4, H2S, NH3, various short-chain hydrocarbons, and a small

amount of aromatic hydrocarbons and tars [5]. In general, the gas phase

has greater hydrogen, oxygen, and sulfur content than the original feed

material, while the remaining solid material (char) is a mixture of carbon-

rich organics and any minerals that were present in the feedstock.

7/29/2019 SK_052_B.doc

7/8

According to the reactions net enthalpy of reaction at 298K is 319.1 kJ/mol

. The temperature inside the gasifier is 1310K.So the enthalpy of reaction

at 1310 K can be calculated by following :

H1310 =H298 + Mp CpT

So Mp CpT=3162.539*10^6 KJ

Hrxn=8268.1392*10^6 KJ

Low grade coal used as fuel souce.

HHV=3700 Kcal/Kg

HHV=3700*4.186 =15466 KJ/Kg

Hrxn=m*HHV

m= 534.601 Ton/day

Mass of low grade coal

HEAT EXCHANGER (E4)

Mi CpiT=MCpTc

(34.56*4.186+24.38*1.029+96.42*14.42+2134.81*1.043+0.671*45.79+

21.25*29.09) *1000*604 = M* 2.2*1000* (700-30)

7/29/2019 SK_052_B.doc

8/8

M=1.818 Ton/hr

Cooling Fluid Used: DOWTHERM-A (Mass used=M)