Fyp.pptx

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PRODUCTION OF LIQUID FUELS USING SYNGAS PRODUCED BY GASIFICATION OF COAL BY FISCHER TROPSCH SYNTHESIS

GROUP MEMBERS

Syed Najeeb Muhammad Subhani Muhammad Salman Muhammad Ukasha Usman* Hafiz Hussnain Akhtar Muhammad Awais

2014-CH-360 2014-CH-351 2014-CH-332 2014-CH-335 2014-CH-343

PROJECT UNDER THE SUPERVISION

DR. AZAM SAEED ENGR. FAISAL REHMAN

INTRODUCTION

PRODUCT INTRODUCTION

DIESEL

Carbon range C5---C12 . Offers a wide range of performance, efficiency, and safety features.

 Diesel fuel also has a greater energy density than other liquid fuels. Provides more useful energy per unit of volume.

GASOLINE Light-duty vehicles (cars, sport utility vehicles, and small trucks) account for about 90% of all gasoline consumption in the United States. Considered as a more cleaner fuel than diesel. Demand increasing more than diesel.

DIESEL

GASOLINE

 FT Diesel has a higher cetane number, approaching 70.

 FT gasoline has a boiling range from 100-400 °F°

 Sulfur content is potentially zero, with almost zero or minimal NOx and SOx.

The Net Heating value is 46.4 MJ/Kg

 Heating value of FT diesel is 45.6 MJ/Kg

CTL PROCESS

GTL PROCESS

BTL PROCESS

 A CTL plant based on  Converts natural gas-  Use any Biomass indirect liquefaction. the cleanest burning residues or organic  Fischer-Tropsch fossil fuel- into high wastes such as synthesis would quality liquid trees, perennial produce extremely products. grasses, straw, bark, clean-burning liquid  GTL products are bagasse, waste paper, hydrocarbon products. colorless and odorless. reclaimed wood or  Products are virtually  Our country facing fiber based free of sulfur, shortage of natural gas composites. nitrogen, and aromatic so we can’t use this compounds, such as process. benzene, and that are compatible with the existing transportation fuel distribution.

8

Why CTL ?  Availability of Coal  Abundant resources in Pakistan  A CTL plant based on indirect liquefaction and Fischer-Tropsch synthesis would produce extremely clean-burning liquid hydrocarbon products that are virtually free of sulfur, nitrogen, and aromatic compounds, such as benzene, and that are compatible with the existing transportation fuel distribution

9

Direct Liquefaction  Direct Liquefaction (DL) is similar to hydrocracking processes used in petroleum refining to convert heavy oils into gasoline and diesel fuel  . The direct liquids must be further upgraded to produce liquid fuels.  . The hydrogen required can be produced within the liquefaction facility by means of coal gasification and the water-gas shift reaction  . The thermal efficiency for direct liquefaction is about 55%.

Indirect Liquefaction  Indirect Liquefaction (IL) is a multi-step process for the production of liquid fuels.  Coal gasification is the first step in indirect liquefaction. The intermediate product produced by gasification is referred to as syngas.  The water-gas-shift reaction both rejects carbon (by converting CO to CO2) and adds H2 (by converting H2O to H2).  . Liquid Hydrocarbons can be produced from syngas via the Fischer-Tropsch (FT) synthesis over either an iron or cobalt-based catalyst 10

WHY FT?

 F-T diesel has a cetane number over 70  F-T diesel contains virtually no sulfur, lean NOx aftertreatment catalysts can be used to reduce engine NOx emissions.

 F-T diesel in engines have shown that hydrocarbon emissions can be reduced by almost 43% compared to petroleum diesel

.

 This wax is of extremely high quality and can be sold as a specialty product, or can be cracked to produce additional F-T diesel.

11

PROCESS DESCRIPTION

PROCESS DESCRIPTION

Syngas Production – This section of the plant includes coal handling, drying and grinding, followed by gasification. An air separation unit provides oxygen to the gasifier. Synthesis Gas Conversion – This section of the plant includes water-gas shift, a synthesis-gas conversion reactors, CO2 removal. The clean synthesis gas is shifted to have the desired hydrogen/carbon monoxide ratio, and then catalytically converted to liquid fuel. Acid gas removal For all systems the acid gases CO2, H2S, and COS contained in the syngas are removed CO2 removal is required to improve the kinetics and economics of the downstream synthesis process. H2S removal is required (to much lower levels than is required for power generation applications) to avoid poisoning of the synthesis catalyst.

PROCESS DESCRIPTION F-T Synthesis: In our designs, we utilize a slurry-phase F-T synthesis reactor with an iron catalyst. reactors. The advantage of an iron catalyst over cobalt for converting coal-derived syngas is that iron has water-gas shift activity and internally adjusts the low H2/CO ratio of the coal derived syngas to that required by the FT synthesis reaction

PROCESS FLOW DIAGRAM

15

16

CAPACITY SELECTION

SECTOR WISE OIL CONSUMPTION IN PAKISTAN

More than 91%of the oil consumption in FY 16 took place in two sectors :transport(48.8%) and power (42.7%)

Pakistan Gasoline consumption by Year 100 90

Thousand barrels per day

80 70 60 50 40 30 20 10 0 1980

1985

1990

1995

2000

2005

2010

2015

2020

Year Indexmundi.com/Pakistan

19

Pakistan diesel consumption per year 180

160

140

1000 BBL/ day

120

100

80

60

40

20

0 1980

1985

1990

1995

2000

2005

2010

2015

2020

Year Indexmundi.com/Pakistan

20

World Gasoline consumption by year 30000

Thousand barrels per day

25000

20000

15000

10000

5000

0 1980

1985

1990

1995

2000

2005

2010

2015

2020

Year Indexmundi.com/Pakistan

21

World's diesel consumption by year 30000

Thousand barrels per day

25000

20000

15000

10000

5000

0 1980

1985

1990

1995

2000

2005

2010

2015

2020

year Indexmundi.com/Pakistan

22

OIL DEMAND FORECAST

The steady increase in population , the changes in life style of people and prices of petroleum products will result in an increase in oil consumption in the coming years. If the local crude production and refining capacity do not increase then Pakistan has to increasingly rely on imports to meet its oil demand 30 29

MMTOE

28 27 26 25 24 23 22 2015

2016

2017

2018

2019 2020 YEAR

2021

2022

2023

2024

Pakistan petroleum products consumption and production by year 600

THOUSAND BARRELS PER DAY

500

400

300

200

100

0 1980

1984

1988

1992

1996

2002

2006

2008

2009

2010

2011

2012

2013

2014

2015

2016

YEAR consumption production

Indexmundi.com/Pakistan

24

 Pakistan annual diesel consumption is 8 million metric ton. More than half of requirement is met through direct diesel import. Rest is produced by local refineries through import of crude. Pakistan daily diesel production is 90,000 BBL/day.

25

 Pakistan relies heavily on import of liquid fuels to fulfill its requirements.  A minimum of 65000 BBL/Day diesel is imported from gulf and other regions.  Also Pakistan has abundant resources of low grade lignite coal in Thar and other parts of Pakistan.  Using the lignite coal, we have tried to reduce the daily import to 35% by producing 42568 BBL of FT diesel per day

26

COAL RESERVES IN PAKISTAN

Province

Resources (Million tones)

Heating Value (BTU/lb)

SINDH

184,623

5219-1355

BALOCHISTAN

217

9637-15499

PUNJAB

235

9472-15801

NWFP

91

9386-14217

AJK

9

7336-12338

TOTAL

185,175

27

Thar Lignite Coal Ultimate Analysis

Component

Fraction(%)

C

36.39

H

4.21

O

7.76

N

0.64

S

2

Ash

14

Moisture Content

35

28

Material Balance

29

Gasifier Main Reactions C + .5O2

CO

C + H2O

CO + H2

C + CO2

2CO

C + 2H2

CH4

CH4 + H2O

CO + 3H2

H2 + C + N2

2HCN

HCN + H2O

CO + NH3

H2

H2S

+S

H2O + .5O2

H2O

CO + .5O2

CO2

CO + H2O

CO2 + H2O

CO + S

COS 30 30

Operating Conditions • Temperature=1500K • Pressure=75 barr

31

Material Balance across Gasifier Inlet Fraction

Mass (Kg/hr)

Kmol

Outlet

Moles (Kmole)

Mass (Kg/hr)

Weight fraction

C

0.48

343915

28659.6

CO

18887.8

528858.6

0.52

H2

0.06

40183

19932.04

N2

0.009

6106.1

218.1

H2

33601.7

67741.1

0.07

S

0.03

20020

625.6

CO2

8168.3

359406.7

0.35

O2

0.10

74074

2314.8

NH3

5.9

100.8

9.92E-05

H2O

0.13

95566.9

5309.3

H2S

606.8

20633.1

0.02

Ash

0.19

135135

HCN

28.96

781.9

0.0007

COS

18.8

1126.1

0.001

CH4

730.8

11693.1

0.01

N2

200.6

5617.6

0.006

20145.7

0.02

O2 kg/hr 237632.9 H2O (g) kg/hr 188141.2

S1

S4

Gasifier

S2 S5 S3

Slag (Kg/hr)

SOLIDS

TOTAL MASS IN (Kg/hr)

TOTAL MASS OUT Kg/hr)

1.1 * 106

1.1 * 106 32

124888.1

Wet Scrubber  Wet scrubbers are particularly useful in the removal of PM with the following characteristics: • Sticky and/or hygroscopic materials (materials that readily absorb water); • Combustible, corrosive and explosive materials; • Particles which are difficult to remove in their dry form; • PM in the presence of soluble gases; and

• PM in waste gas streams with high moisture content 33

Material balance across Scrubber Water Flowrate (Kg/hr) Outlet

Mass (Kg/hr)

Weight fraction

CO

528858.6

0.53

CO2

359406.6

0.36

H2S

20632.9

0.02

CH4

11693.1

0.01

H2

67741.1

0.06

N2

5617.6

0.006

51.45

Inlet

Mass (Kg/hr)

Weight fraction

CO

528858.6

0.52

H2

67741.1

0.06

CO2

359406.7

0.35

NH3

100.8

0.00001

H2S

20633.1

0.02

HCN

781.9

COS

S8

Venturi Wet Scrubber

S7

S9

S 10 Outlet

Mass (Kg/hr)

Weight fraction

0.0007

CO

0.001

5.6E-08

NH3

30.2

0.00003

1126.1

0.001

0.000002

0.01

3.1E-06 6.9E-06 4.3E-08

2.1

11693.1

0.06 0.1 0.0009

H2O

CH4

CO2 H2S CH4

Particle

2014.6

0.002

5617.6

0.006 0.019

Total

1016105

1

0.002 3.6E-09 0.004 3.9E-08 0.04 0.05 0.9

1

20145.7

49.3 0.00007 70.6 0.0008 781.9 1126.1 18131.

995996.9

Solids

H2O H2 NH3 N2 HCN COS Particle Total

Total

N2

20159.3

1

Total Mass in (Kg/hr)

Total Mass out(Kg/hr)

1.0 * 106

1.0 * 106 34

Water Gas Shift Reactor  The product from gasifier has a H2 / CO ratio of 1.6.  For proper synthesis in FT reactor, H2 /CO ratio must be more than 2, so a water gas shift reactor is installed.  Steam is added, the ratio of entering steam and CO, CO/H2O is set to be 1/2.  A Fe2O3/Cr203 Catalyst is used, because a high temperature shift is required due to presence of H2S content in the gas.  With 38% conversion at 598.15K , the new H/CO ratio becomes 3.2.

598.15 k CO + H20

CO2 + H2 Fe2O3/Cr203 35

Material balance across Water Gas Shift Reactor

Inlet

Mass (Kg/hr)

CO CO2

528858.5 359406

H2

67741.01

CH4 NH3 N2

11693.1 30.2 5617.6

H2S

20632.9

PM H2 O

2039.2 2.1

Total

996020.7

Inlet

H2 O Total

Flowrate (kg/hr) 679960.8 679960.8 S 12

Water Gas Shift Reactor S 11

S 13

Outlet

Mass (kg/hr)

CO CO2

317315.1 675210.1

H2

78929.2

CH4 NH3 N2

17737.2 30.2 5617.6

H2 S

20632.9

PM H2 O

2039.2 557570.1

Total

1675981.6

TOTAL MASS IN (Kg/hr)

TOTAL MASS OUT (Kg/hr)

1.7 * 106

1.7 * 106

36

Absorber Absorber is used to remove acid gases in syn-gas stream, Because Acid gas is extremely poison and harmful to humans. In addition the removal of acid gases is necessary because of:

 Their removal is further justified by the corrosion effects.  H2S can be converted to elemental sulfur.  Acid gases are extremely poisonous and very harmful to humans.  Their pungent odor males their presence very undesirable.  MDEA has the potential to absorb 98% H2S ,90% CO2, 99% CH4, 100% H2O (at 25 °C)

37

Material balance across Absorber Outlet MDEA Mass flow rate (kg/hr)

Molar flow rate (kgmol/hr)

MDEA Concentration

1073587.1

1805.1

23%

S15

S 17

Moles (kmoles)

Mass (Kg/hr)

Weight fraction

CO CO2

11219.4 1534.6

314141.9 67521.01

0.67 0.14

H2 CH4 NH3 N2 H2S Total

39914.6 5.5 1.8 200.6 6.1 52882.6

79829.3 88.7 30.3 5617.6 206.3 467435

0.17 0.0002 0.00006 0.01 0.0004 1

Outlet

Moles (kmoles)

Mass (kg/hr)

Weight fraction

Inlet

Moles (kmole)

Mass (kg/hr)

Weight fraction

CO

11332.7

317315.1

0.19

CO2

15345.7

675210.1

0.40

H2

39914.6

79829.3

0.047

CO

113.3

3173.2

0.003

CH4

1108.6

17737.2

0.01

CO2

13811.1

607689.1

0.50

NH3

1.8

30.2

0.000018

CH4

1103

17648.5

0.01

N2

200.6

5616.8

0.003

H2S

600.8

20426.6

0.01

H2S

606.9

20632.9

0.01

Particle

2039.2

0.002

2039.2

0.001

Particle H2O

30976.1

557570

0.33

Total

99486.9

1675981

1

Absorber

S 14

S 16

H2O

30976.1

557570.1

0.46

Total

46604.3

1208546

1

TOTAL MASS IN (Kg/hr)

TOTAL MASS OUT (Kg/hr)

1.7 * 106

38 6 1.7 * 10

Pressure Swing Adsorption  Pressure swing adsorption (PSA) is a technology used to separate some gas species from a mixture of gases under pressure according to the species' molecular characteristics and affinity for an adsorbent material.

 Specific adsorptive materials (e.g., zeolites, activated carbon, molecular sieves, etc.) are used as a trap, preferentially adsorbing the target gas species at high pressure. The process then swings to low pressure to desorb the adsorbed material.

 Activated Carbon has affinity to adsorb (Methane, Carbon dioxide and Moisture) & Zeolite has affinity to adsorb (Carbon monoxide, Ammonia and Nitrogen). 39

Material balance across PSA

Inlet

Moles (Kmole)

Mass (Kg/hr)

Weight fraction

CO

11219.3

314141.9

0.67

CO2

1534.6

67521

0.14

H2

39914.6

79829.3

0.17

CH4

5.5

88.7

0.0002

NH3

1.8

30.3

0.00006

N2

200.6

5617.6

0.01

H2S

6.1

206.3

0.0004

Total

52882.6

467435

1

Outlet

PSA S 17

S 18

Moles (kmole)

Mass (kg/hr)

Weight fraction

CO

11219.3 314141.9

0.8

H2

39914.6

0.2

Total

79829.3

51133.9 393971.1

1

Total Mass In (Kg/hr)

Total Mass Out (Kg/hr)

Adsorbed Mass (Kg/hr)

4.6 * 105

3.9 * 105

7.3 * 104 40

FT Reactor • FT synthesis is typically carried out in the temperature range of 210-340 °C and at high pressure (15-20) barr.

• The product range includes hydrocarbons (CH4C2H6),propane(C3H8), butane(C4H10), gasoline(C13-C17) , diesel(C5-C12) , and waxes(+C19).

• All reactions are exothermic and product is a mixture of different hydrocarbons mainly consisting of parrafins and olefins

• nCO + (2n+1)H2

CnH2n+2 + nH2O 41

Material balance across FT Reactor Outlet

Inlet

CO

Moles Mass Weight (Kmoles) (Kg/hr) fraction

11219.3

314141.9

0.79

H2

39914.6

79829.3

0.21

Total

51134

393971.1

1

S 19

FT REACTOR

S 20

C3-C4

10%

37427.3

Gasoline

25%

93568.2

823.4

Diesel

30%

112281.8

988.1

Soft Paraffin Wax

20%

74854.5

658.7

Hard Paraffin Wax

15%

56140.9

494

Total

100%

374272.6

3293.6

Outlet TOTAL MASS IN Kg/hr)

TOTAL MASS OUT (Kg/hr)

3.9 * 105

3.9 * 105

CO Conversion 95%

Mass Mass Composition (Kg/hr) (BBL/hr)

Mass (kg/hr)

CO

656.6

H2

328.3

H2O

18713

42

Distillation Column  The product from FT has 4 components, with C3-C4 being the lightest, and waxes being the heaviest of them.  Considering gasoline as our Light key in the first column, it has a boiling point range of 35-200 °C.  Setting the temperature of first column to 200 °C and taking sharp split into account,  99% of gasoline is recovered the distillate.  In the second column where now diesel is the light key, setting the temperature to 320 °C, 99% of diesel is recovered from the distillate.  Waxes both soft and hard are recovered as the bottom product. 43

Material balance across Distillation Column 1

S 21 Inlet

Mass (Kg/hr)

BBL/hr

C1-C4

37427.3

329.4

Gasoline

93568.2

823.4

Diesel

112281.8

988.07

Soft wax

74854.5

658.7

wax

56140.9

494.0

Distillation column 1

Outlet

Distillate (Kg/hr)

C1-C4

37427.3

Gasoline

92632.5

Diesel

1122.8

Soft wax

0

wax

0

Outlet

Bottom (Kg/hr)

C1-C4

0

Gasoline

935.7

Diesel

111159

Soft wax

74854.5

wax

44 56140.9

S 20

S 22 Total Mass In (Kg/hr)

Total Mass Out (Kg/hr)

3.7 * 105

3.7 * 105

Material balance across Hydrocracker

Inlet

Kg/hr

Gasoline

935.6815

Diesel

111159

Soft wax

74854.52

wax

56140.89

Total

243090.1

S 25’

Outlet

Outlet (kg/hr)

C1-C4

16138.64

gasoline

20008.61

Diesel

203589.3

Hydrocracker Total

S 23’ Unconverted

258809.5

19072.93

S 24’ H2 enter

Total Mass In (Kg/hr)

Total Mass out (Kg/hr)

2.5 * 105

2.5 * 105

15719.45 (kg/hr)

45 45

Material balance across Distillation Column 2

S 25 Inlet

Gasoline

Mass (Kg/hr) 935.7

BBL/hr

Distillation column 2

8.233997

Diesel

111159

978.1989

Soft wax

74854.5

658.7198

wax

56140.9

494.0398

S 23

S 24

Total Mass In (Kg/hr)

Total Mass out (Kg/hr)

2.4 * 105

2.4 * 105

Outlet

Distillate (Kg/hr)

Gasoline

935.7

Diesel

110047.4

Soft wax

0

wax

0

Outlet

Bottom (Kg/h)

Gasoline

0

Diesel

1111.6

Soft wax

74854.4

wax

56140.9

46

Overall Material Balance S8

S12

S15 S21 S24 S25

S1 CTL PLANT

S2 S3 S5

S9

S16

S18’

S20’

Inlet Stream No.

Mass (Kg/hr)

Outlet Steam No. Mass (Kg/hr)

S1

715000

S5

124888.1

S2

237632.9

S9

20159.3

S3

188141.2

S16

2282133.1

S8

51.45

S18’

73463.9

S12

679960.8

S20’

19698.56

S15 Total Mass In

1073587.1 Total Mass Out

S21

131182.6

2894373.4 Kg/hr

2894373.4 Kg/hr

S24

131358.5

S25

111731.6

47

Overall Material Balance

Total Coal In (Kg/day) 17160000

C1-C4

1281708 Kg/day

Gasoline

4183

BBL/day

Diesel

42568

BBL/day

Wax

457750 Kg/day

48

Energy Balance

49

Energy balance across Gasifier

Outlet

Cp (kJ/kg)

Mass (Kg/hr)

Q 106(KJ/hr)

CO

1.1

528858.6

730.4

CO2

1.2

359406.7

500.9

H2

15.0

67741.1

1224.5

Inlet

Cp (kJ/kg)

Mass (Kg/hr)

Qin 106(KJ/hr)

C

0.7

343915

3.8

H2

14.3

40183

8.6

H2S

1.3

20633.1

31.6

N2

1.0

6106.1

0.1

N2

1.1

5617.6

7.7

O2

0.1

74074

1.02

CH4

5.1

11693.1

72.05

S

0.7

20020

0.21

100.8

0.29

4.2

95566.9

6.02

NH3

2.4

H2O Ash

1.4

135135

2.83

Particle

1.4

20145.7

33.9

Total

2.1

715000

22.7

HCN COS

1.8 1.0

782 1126.1

1.7 1.4

Total

2.1

1016104.7

2604.4

Inlet O2

Cp Mass Qin (kJ/kg) (Kg/hr) 106(Kj/hr) 1.1 237632.9 327.3 Q H2 O 106( KJ/hr) 606.7

S1

S4

Gasifier S2

S5 S3

Outlet

Q out 106 (KJ/hr)

Slag

210.8

IN-OUT+GENERATION+CONSUMPTION=ACCUMULATION (956.7 * 106 ) – (2815.2 * 106) + (1858.5 * 106) + 0=0 IN+GENERATION=OUT

50

Energy balance across Scrubber Water Q (Kj/hr)

Cp (Kj/kg)

Q in 6 10 (KJ/hr)

Inlet

Mass (kg/hr)

CO

528858.6

1.1

83.9

H2

67741.1

14.4

146.5

CO2

359406.7

0.9

50.7

NH3

100.8

2.2

0.03

H2S

20633.1

HCN

781.9

COS CH4

N2

1126.1 11693.1

5617.6

Particles 20145.7 Total

1016105

1.1

0 (at 25° C)

S8 Venturi Wet Scrubber S9

S7

3.3

Outlet CO

S 10

Mass (Kg/hr)

Cp (Kj/kg

0.001

1.0

Cp (Kj/kg)

Outlet

Mass (Kg/hr)

Qout 6 10 (KJ/hr)

CO

528858.6

1.0

16.6

CO2

359406.6

0.9

9.4

H2S

20633

1.0

0.6

CH4

11693.1

2.3

0.8

H2

67741.1

14.5

29.7

N2

5617.6

1.0

0.2

0.2

CO2

0.06

0.9

0.1

H2S

0.1

1.0

NH3

2.1

0.002

4.4

0.0009

2.3

30.3

CH4

49.3

1.9

H2O

2.1

1.9

0.0001

0.9

H20

14.4

2014.6

1.5

0.09

5.1

0.00007

Particle

1.7

H2

1.93

295.1

NH3

70.6

2.2

Total

995996.9

1.9

57.3

N2

0.0008

1.0

HCN

781.9

1.4

CoS

1126.1

0.7

Particle

18131.1

1.8

1.4 0.7 2.5

1.0

Qout 106(KJ/hr)

240.3

51

IN-OUT+GENERATION+CONSUMPTION=ACCUMULATION (297.6 * 106 ) – (297.6 * 106 )+ 0 + 0 = 0 IN=OUT

52

Energy balance across Water-Gas shift reactor

Inlet

Mass (kg/hr)

Outlet

Cp Qin (Kj/kg) 106(KJ/hr) Inlet

Mass Cp Qout (kg/hr) (Kj/kg) 106(KJ/hr)

CO

317315.1

1.1

264.7

CO2

675210.1

1.1

555

2055.81

H2

78929.2

14.7

887.4

2055.81

CH4

17737.2

3.4

46.6

NH3

30.25

2.6

0.06

N2

5617.6

2.2

9.3

H2S

20632.9

1.2

18.4

PM

2039.18

1.5

2.2

557570.1 1675081. 6

2.1

86.7

2.0

2651.6

Mass (kg/hr)

Qin 106(KJ/hr)

H20

679960.8

Total

679960.8

CO

528858.5

1.1

169.98

CO2

359406

0.1

107.5

H2

67741.1

14.5

294.4

CH4

11693.1

2.8

9.8

NH3

30.3

2.4

0.02

N2

5617.6

2.1

3.6

H2S

20632.9

1.1

6.8

PM

2039.2

1.5

0.89

H2O

2.1

1.9

0.001

H2O

Total

996020.7

1.9

592.8

Total

S 12 S 11

S 13

Water Gas Shift Reactor

IN-OUT+GENERATION+CONSUMPTION=ACCUMULATION (2338.6 * 106 ) – (2311.9 * 106) + ( 3.1 * 106) + 0=0 IN+GENERATION=OUT

53

Energy balance across Absorber Inlet

Mass Kg/hr

Cp (Kj/kg)

Qin 106(Kj/hr)

MDEA soln.(23%)

10730 52.09

3.76

101.3

Inlet

S 15

Mass Cp Qout Outlet (Kg/hr) (Kj/kg) 106(Kj/hr)

Qgeneration (1160.5 Kj/hr)

CO

314141.9

1.0

13.5

CO2

67521.1

0.9

2.42

H2S

206.3

1.0

0.009

CH4

88.7

2.3

0.008262

S 16

H2

79829.3

14.6

47.7

Mass Cp Qout 6 (Kg/hr) (Kj/kg) 10 (Kj/hr)

N2

5617.6

1.0

0.2

NH3

30.3

2.1

0.003

Total

467435

3.3

63.9

S 17 Absorber

Mass Cp Qin 6 ( Kg/hr) (Kj/kg) 10 (Kj/hr)

CO

317315.3

1.04

3.3

CO2

675210.1

0.9

5.8

H2

79829.3

14.4

11.5

Outlet

H2S

20632.9

1.0

0.2

CO

3173.151

1.0

0.14

N2

5616.8

1.0

0.06

CO2

607689.1

0.9

22.4

CH4

17737.2

2.2

0.4

H2S

20426.57

1.0

0.9

NH3

30.1

2.1

0.0006

CH4

17648.51

2.3

1.7

H2O

557570

1.9

10.4

H2O

557570.1

1.9

43.8

particle

2039.2

1.5

0.03

Particle

2039.18

1.53

0.13

Total

1675981

26.04

1.89

Total

1208547

1.4

69.1

S 14

54

IN-OUT+GENERATION+CONSUMPTION=ACCUMULATION (133 * 106 ) – (133 * 106) + (1160) + 0=0 IN+GENERATION=OUT

55

Energy balance across PSA

Inlet

Mass (Kg/hr)

Cp (Kj/kg

Qout 6 10 (KJ/hr)

CO

314141.9

1.0

4259019

CO2

67521.1

0.9

0.8

H2S

206.3

1.0

0.003

CH4

88.7

2.3

0.003

H2

79829.3

14.6

15.2

N2

5617.6

1.0

S 17

PSA

S 18

Cp (KJ/kg

Outlet

Mass (kg/hr)

Qout 106(KJ/hr)

CO

314141.9

1.0

4.3

H2

79829.3

14.6

15.2

Total

393971.1

3.8

19.5

0.08

NH3

30.3

2.1

0.0008

Total

467435

3.3

20.2

IN-OUT+GENERATION+CONSUMPTION=ACCUMULATION (63.9 * 106 ) – (63.9 * 106) + 0 + 0=0 IN=OUT 56

Energy balance across FT-Reactor

Outlet

Inlet

Mass (kg/hr)

Cp Qin (KJ/kg) 106(KJ/hr)

S 19 CO

H2

Total

314141.9

79829.3

393971.2

1.1

14.4

3.8

64.01

FT REACTOR

S 20

Mass (kg/hr)

Cp (KJ/kg)

Qout 106(KJ/hr)

Propane 18171.3

2.5

16.8

Butane

18171.2

2.4

16.6

Gasoline 90856.1

2.4

81.7

109027.3

2.3

94.1

Soft Wax 72684.9

2.4

65.4

Hard Wax 639.6 CO 328.31

2.5

0.6

1.1

0.1

14.4

3.5

1.9

4.5

2.4

283.4

Diesel

221.2

H2

656.62

H2O

6237.8 8

285.2

Total

316773

IN-OUT+GENERATION+CONSUMPTION=ACCUMULATION (285.2 * 106 ) – (283.2 * 106) + (1.8 * 106)+ 0=0 IN=OUT 57

58