Material Balance Ulsd Reactor Talha

8/12/2019 Material Balance Ulsd Reactor Talha

1/16

mercaptan

sulphide

disulphide

cyclic sulphide

thiopene

linear olefin

Cyclic olefins

Aromatic saturation

Basis

30000

30000bbl 1 Day 5.6145835ft3

Day 24 hrs 1 bbl

REACTOR

C-C-S-C-C+2H2 2C-C + H2

C-C-C-C-SH+ H2 C-C-C-C-H + H2S

By knowing the API gravity of diesel at reactor inlet, the ma

Capacity of diesel we selected =

Degrees API0 at 600F = 32.8

Specific Gravity = 141.5 / (32.8 + 131.5) = 0.861

Density of water at 600F = 62.37 lb/ft3

C-C-S-S-C-C + 3H2 2C-C + 2H2S

Reactions occurring in the reactor

Reactions of sulfur compounds

Reactions of olefins saturation

C-C-C-C=C-C-C + H2 C-C-C-C-C-C-C

Density of diesel at 600F = 0.861 x 62.37 = 53.71 lb/ft3

Mass flow rate of diesel at 600F = 7720.0523 x 53.71 =


2/16

376641.4lb 0.453592kg 170841.5146 kg/hrhr 1lb

2425.94951 kg/hr

485.1899014 kg/hr

moles of S molar mass of S mass of S moles of H2

molar

mass of

H2

merceptan 1 32 32 1 2

sulphide 1 32 32 2 2

disulphide 2 32 64 3 2

cyclic

sulphide1 32 32 2 2

thiophene 1 32 32 4 2

6833.66058 kg/hr

3416.83029 kg/hr

moles of

olefin

molar mass of

olefinmass of olefin moles of H2

molar

mass of

H2

Linear

Olefin1 80 84 1 2

Olefin 1 84 80 2 2

Amount

Olefin Saturation Produce =

For Sulfur Compounds

Sulfur Composition in feed = 1.42%

Total feed of diesel entering in reactor = 170842kg/hr

Olefin Saturation

Olefins Composition = 4%Total feed of diesel entering in reactor = 170842kg/hr

Total Sulfur =

Total sulfur reactions = 5

Sulfur for each reaction =

Halide Removal

Halide composition = 2.5%


Total reactions = 2

For each reaction =


3/16

4271.03786 kg/hr

moles of

halide

molar mass of

halidemass of halide moles of H2

molar

mass of

H2

halide 1 154.5 154.5 1 2

2106.395394 kg/hr

1053.197697 kg/hr

3159.59309 kg/hr

mass of S mass of H2 mass of Smass of H2S produces

(kg/hr)

merceptan32 34 485.1899014 515.5142702

sulphide32 34 485.1899014 515.5142702

disulphide 32 68 485.1899014 1031.02854cyclic

sulphide 32 34 485.1899014 515.5142702

thiophene32 34 485.1899014 515.5142702

3093.085621

mass of

compoundmass of C2

mass of

compound

mass of C2 produces

(kg/hr)

sulphide 32 60 485.1899014 909.7310651

disulphide 64 60 485.1899014 454.8655325

1364.596598

C2 produced

H2S produced in the reactor

Total Halides =

Total H2 required for all reactions =

By taking 50% H2in excess =

Total H2 entering in reactor =


4/16

mass of

compoundmass of C2

mass of

compound

mass of C2 produces

(kg/hr)

merceptan 32 58 485.1899014 879.4066962

cyclic

sulphide32 58 485.1899014 879.4066962

thiophene 32 58 485.1899014 879.4066962

pyrrole 67 58 1423.679288 1232.438787

3870.658875

mass of

compoundmass of H2O

mass of

compound

mass of C5+ produces

(kg/hr)

phenol 108 18 22209.39689 3701.566149

3701.566149

Feed in= F1 + F2 = 174001.1

feed out = F3 = 174162

H2

F2(kg/hr) 3159.59309

sulphurcompound

2425.949507

nitrogen

compound4271.037864

olefins 6833.660583

halide 4271.037864

paraffins 108621.035

aromatics 44418.79379

from phenol

Overall Mat

F

Water produced in reactor

C4 produced


5/16

F1(kg/hr) 170841.5146


6/16

pridine

quinoline

pyrrole

bbl/day

7012.5ft3/hr

376641.375lb/hr

ss flow rate of diesel is calculated as follow

Reactions of nitrogen compou

Reactio

HCl +NH3


7/16

4271

mass of Smass of

H2

mass of H2

required

(kg/hr)

moles of Nmolar

mass of N

485.189901 2 30.3243688 pyridine 1 79

485.189901 4 60.6487377 quinoline 1 129

485.189901 6 45.4865533 pyrrole 1 67

485.189901 4 60.6487377

485.189901 8 121.297475

318.405873

mass of

olefin

mass of

H2

mass of H2

required

(kg/hr)

moles of

aromatic

saturation

molar

mass of

aromatic

saturation

3416.83029 2 81.3531022 aromatics 1 78

3416.83029 4 170.841515 phenol 1 94252.194617

f Hydrogen RequiredNitrogen Compounds

Nitrogen Compo

Total feed of

Aromatic Saturation

Aromatics Composition = 26%Total feed of diesel

Total Aromatic Saturation co

Total Nitrogen =

Total nitrogen reactio

Nitrogen for each reaction =

Total Reactions = 2

For each reaction =


8/16

mass of

halide

mass of

H2

mass of H2

required

(kg/hr)

4271.03786 2 55.288516

55.288516

mass of

compoundmass of NH3 mass of S

mass of

NH3

produces

(kg/hr)

pyridine 79 17 1423.679 306.3614

quinoline 129 17 1423.679 187.6167

pyrrole 67 17 1423.679 361.2321

855.2101

mass of

compound

mass of

HClmass of halides

mass of

HCl

produces

(kg/hr)

halide 154.5 36.5 4271.037864 1009.015

1009.015

108621.035 kg/hr

108621.035 kg/hr

C5+ produced

Paraffin composition = 63.58%


Total paraffins =

C5+ present in paraffins =

HCl produced in reactor

Ammonia produced in the reactor (from N2 rem


9/16

mass of

compound

mass of

C5+

mass of

compound

mass of

C5+

produces

(kg/hr)

pyridine 79 72 1423.679288 1297.53

quinoline 129 116 1423.679288 1280.208

2577.738

mass of

compound

mass of

C5+

mass of

compound

mass of

C5+

produces

(kg/hr)Linear

Olefin84 86 3416.830291 3498.183

Olefin 80 84 3416.830291 3587.672

7085.855

174001.108

H2 1053.197697

H2S 3093.085621

NH3 385.257688

NH4Cl 1478.967804

H2O 3701.566149

C2 1364.596598

C4 3870.658875

erial Balance on reactor

ed in = Feed out

From Olefins Compound

From N2 Compound

Reactor


10/16


11/16

ds

ns of halide

NH4Cl


12/16

kg/hr

1423.679288 kg/hr

mass of N moles of H2

molar

mass of

H2

mass of Nmass of

H2

mass of

H2

required

(kg/hr)

79 5 2 1423.679 10 180.2126

129 4 2 1423.679 8 88.29019

67 4 2 1423.679 8 169.9916

438.4943

44418.79379 kg/hr

22209.39689 kg/hr

mass of aromatic

saturationmoles of H2

molar

mass of

H2

mass of

olefin

mass of

H2

mass of

H2

required

(kg/hr)

78 1 2 22209.4 2 569.4717

94 1 2 22209.4 2 472.5404

1042.012

sition in feed = 2.5%

diesel entering in reactor = 170842kg/hr

entering in reactor = 170842kg/hr

mpounds =

s = 3


13/16

855.2101 kg/hr

17 Kg/kgmole

50.30647 kgmole/hr

Total HCl = 1009.015 kg/hr

molar mass of HCl= 36.5 Kg/kgmole

moles of HCl= 27.64426 kgmole/hr

27.64426 kgmole/hr

1478.968 kg/hr

Free NH3 = 22.66222 Kg/kgmole

Free NH3 = 385.2577 kg/hr

mass of

compound

mass of

C5+

mass of

compound

mass of

C5+

produces

(kg/hr)

aromatics 78 84 22209.4 23917.81

phenol 78 48 22209.4 13667.32

From Aromatic Compounds

Wt of NH4Cl produced =

NH4Cl produced in reactor

Total Ammonia =

molar mass of ammonia=

moles of NH3=

NH4Cl produced =

oval)


14/16

37585.13

mass ofcompound

mass ofC5+

mass ofcompound

mass of

C5+produces

(kg/hr)

halide 154.5 121 4271.038 3344.955

3344.955

159214.7 kg/hr

From Halide Removal

Total C5+ produce =


15/16

170841.5146 kJ/hr325 oC

30 oC

3.5 KJ/kgoC

176393863.8 KJ/hr

Component

Flow

rate-

m(KJ/H

R)

Cp(Kg/k

goC)

T(oC)

H2 1053.198 14.3 355

H2S 3093.086 4.39 355

NH3 385.2577 2.43 355NH4Cl 1478.968 1.8 355

H2O 3701.566 1.1 355

C2 1364.597 0.59 355

C4 3870.659 3.5 355

C5+ 159214.7 3.5 355

170841.5*3.5*(325-30)

Mass flow rate of feed = mDiesel =Temperature of feed Tdiesel =

Reference of temperature = TR=

Heat present in feed stream F1

Qin Diesel = mDiesel Cp(Tdiesel-TR) =

Cp at 325oC =

Heat generation in reactor can be calcul

Qgeneration = Qout - Qin

Qin = Qin-Diesel + Qin H2

Qin =Qin(Diesel)+Qin(Hydr

Heat entering in reacto

Heat out from reactor

Qout =Qc5+ +Qc4+Qc2+QNH4Cl+

Total heat of reactor, Total Qout=


16/16

3159.593 kJ/hr325 oC

30 oC

14.3 KJ/kgoC

13328743 KJ/hr

189722607.2 KJ/hr

TR(oC) Qout(kJ/hr)

30 4894736.296

30 4413059.91

30 304257.259130 865196.1654

30 1323309.898

30 261661.3976

30 4402874.471

30 181106740.4

197571835.8

197571835.8 kJ/hr

7849228.525 kJ/hr

Energy balance around reactor

Mass flow rate of H2 = MH2 =

ted as follows

gen)

r

NH3+QH2S+QH2O+QH2

Temperature of feed Tdiesel =

Reference of temperature = TR=

Cp at 325oC =

Heat present in H2 Stream F2

Qin-H2 = mH2Cp(T-TR) =

3159.593*14.3*(325-30)

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Material Balance Ulsd Reactor Talha