1. The document describes a Continues Catalytic Reformer (CCR) unit that has two sections: Naphtha Hydro Treating (NHT) and Platforming. 2. The NHT section produces light and heavy naphtha, while the Platforming section produces hydrogen, high octane reformate, and low octane reformate. 3. The document provides details on the equipment in the CCR unit like heaters, reactors, strippers, splitters, and treaters along with operating parameters such as temperatures, pressures, flow rates.

1. “CCR UNIT”
College of Technological studies
Department of Chemical Engineering Technology
To:
•Dr :ebraheem Alhajry & dr: adel alenizy
Student Name:
•Mohammad Abdulqader Alfuraij
•Abdullah Saleh Alajmi

2. Refineries Built
capable of
refining
Mina Abdulla 1958
280,000 (barrels
per day)
Mina Al-Ahmady 1949 450,000 (BPD)
Mina Shuaiba 1966 200,000 (BPD)
KNPC

3. Coverall Helmet Glasses
Shoes Gas mask Gloves
Safety

4. Capacity (%)
Feed Rate
M3/hr BPD
60 71.6 10800
65 77.5 11700
70 83.5 12600
75 89.5 13500
80 95.4 14400
85 101.4 15300
90 107.4 16200
95 113.3 17100
100 119.3 18000
105 125.3 18900
110 131.2 19800
115 137.2 20700
120 143.2 21600
CCR Unit
In CCR unit we have 2 section:
1. NHT (Naphtha Hydro Treating)
2. Platforming
The product from NHT section is :
1. Light Naphtha
2. Heavy naphtha
The product From platforming is :
1. Hydrogen
2. High octane reformate
3. Low octane reformate
Continues Catalytic Reformer

5. BDF
Heater Reactor Striper Splitter
Feed Surge
Dram
Heaters&
Rectors
Separator
Treater
debutanizer
Light Naphtha
Heavy Naphtha
Gas
Liquid
H2 rich gas to
HR unit
H2 to NHT unit
High octane
Reformate
Low octane
Reformate
NHT
Platforming

6. Heater H-101
Feed surge drum V-101
NHT Reactor
V-102
Tanks
Pump P-101
Pump P-110
Heat Exchanger E-101
To Fin fan E-102

7. From E-101 Fin fan E-
102
To E-101
Water to sea
water
Cooler E-103
Separator V-103
Compressor C-
101
To Exchanger E-104

8. From V-103
Exchanger E-105
Fin fan E-106
Cooler E-107
Separator V-106
Pump P-103
Fin fan E-106
Striper V-105
Off gas to main treating
Off gas to
ARD
Watertoseawater
To V-107

9. From E-105
To E-201
(Sweet naphtha)
Fin fan E-109
Reboiler E-110
Pump P-104
Cooer E-111
Cooer E-112
Splitter V-107

10. Rx-4
Rx-3
Rx-2
Rx-1
rectors
Heaters
Exchanger Packinox
From Splitter V-107
To Fin fan E-203

11. From E-201 Fin fan E-203
Water to sea water
Separator V-205
To Pump P-202
Compressor
C-201
Cooler E-204
Treater E-209
(H2 to HR unit)
(H2 to NHT section)

12. High octane
reformate
Low octane
reformate
Cooler E-212 Heater H-205
Cooler E-213
Pump P-202
Exchanger E-211
Debutanizer V-210
LPG production
to FGRU

13. Tests
Streamoil Splitter O/ H Splitter Btm Reformate
Sp.gr 0.6663 0.7419 0.8851
IBP ◦c - 107 34
10% - 114 93
50% - 124 130
905 - 146 166
FBP ◦c - 170 202
RON - - 99.3
RVP 9.4 - 7.8
Stream(water) NHTseparator Stripper boot
PH 7.9 7.7
Iron 0.3 0.8
H2S 42 196
NH3 12 10
Stream(cat) Regancat SPcat
Cl2 1.04 0.87
Cock 0.19 4.7
LPcond
PH 8.3
Cond 5.0

15. Tin put Tout put pressure
315c◦ 320c◦ 21.5kg/cm2
Reactor V-102
•The catalyst use in this reactor is “cobalt molybdenum”
•The reactions in this reactor:
• H2S
• NH3
Naphtha +H2 = 3- H2O
4- Olefin Removal
5- Halide Removal
6- Metal Removal
•The hydrotreated naphtha sulfur content should be maintained well bellow the 0.5 wt ppm
maximum

16. Stripper V-105
Tinput Toutputgas Toutputliquid
133c◦ 83c◦ 197c◦
 This stripper has 25 trays.
 There is used bubble cup in stripper.
 This stripper used to Separates H2Sfrom Naphtha .
 After separate H2Swill go to Amine Unit
 H2Safter separate is 818Nm3/ h.
 Removal of light ends from a liquid by contacting it with an inert medium such as steam or nitrogen.
 Principle : reducing the partial pressure by means of another vapor component and thereby reducing the
boiling point of the liquid mixture.

17. Naphtha splitter V-107
 This splitter has 60 trays.
 The feed is began from tray 25
 There is used bubble cup in splitter.
 This splitter used to Separates light naphtha from heavy Naphtha .
 In product we will have 36% liquid and 64 %gasses.
 The product we have from splitter is 38%light naphtha and 62%heavy naphtha.
Tinput Toutput gasses Toutput pressure
140c◦ 86c◦ 168c◦ 1.5kg/cm2

18. Heaters and Reactors
Heaters Burner From To Tinput Toutput
H-201 10 E-201 Rx-1 460 c◦ 549 c◦
H-202 16 Rx-1 Rx-2 434 c◦ 549 c◦
H203 8 Rx-2 Rx-3 470 c◦ 549 c◦
H-204 6 Rx-3 Rx-4 488 c◦ 549 c◦
 Before any reactor we have heater, so we have 4 reactors and 4 heaters.
 We use heaters to keep Tout constant .
 All heaters is fuel gas heater.
 The catalyst used in reactors is “R232”
Rx-1
H-201
H-202
H-203
H-204
Rx-2
Rx-3
Rx-4
 Platforming Reactors reaction:
1. Naphthene dehydrogenation
2. Naphthene isomerization
3. Paraffin isomerization.
4. Paraffin dehydrocyclization.
5. Hydrocracking.
6. Demethylation.
7. Romatic dealkylation.

19. Chloride Treaters
Temperature Chlorideflowrate Hydrogenflowrate
38c◦ 3680NM3/hr 13NM3/hr
 Its separate chloride from hydrogen.
 Its send chloride to the booster gas coalesce.
 Hydrogen send to NHT unit and HRunit.
 We will send 1350 NM3/ hr to of hydrogen to NHT unit.
 We will send also 39154 NM3/ hr of hydrogen to HRunit

20. Debutanizer V-210
Tinput Ttray30output Tresidueoutput pressure
177c◦ 61c◦ 200c◦ 10.5kg/cm2
 Its separate LPG from Reformate.
 LPG send to FFGRU.
 Its has 30 tray.
 93.6 NM3/ hr product of reformate.