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OCT-M！FCC gasoline selective HDS
Background
FCC gasoline is of high contents of sulfur and olefins. Higher hydrogen consumption and higher octane number loss are the disadvantages of conventional HDS processes. OCT-M！FCC gasoline selective HDS technology is featured by selecting a suitable cutting point and cutting the FCC gasoline feed into two parts, then treating the light and heavy fractions separately. The light fraction normally has high olefin content and low sulfur content(most sulfur-containing substances are low carbon number mercaptans) and will be treated by caustic-scrubbing-extracting. The heavy fraction has high content of sulfur(especially thiophenic sulfur), it should be treated with specialty catalyst under mild operating conditions.
Features
✧ Feed can be of high sulfur, high olefin FCC gasoline
✧ Special HDS catalyst
✧ Mild operating conditions for heavy fractions
✧ High liquid yield(>99%)
✧ Low hydrogen consumption(0.2~0.3%)
✧ Proper cutting point
Aimed at
✧ Feed of FCC gasoline has high sulfur content(1000-1200ppm) and high
olefin contents(30-40%)
while sulfur content requirement to product is lower than 300ppm;
✧ Feed of FCC gasoline has moderate sulfur content(800-1000ppm) and
moderate olefin
contents(25-35%) while sulfur content requirement to product is lower than 200ppm;
Typical results
OCT-M！FCC gasoline selective HDS technology developed in FRIPP, SINOPEC has been put into commercial application in Guangzhou Petrochemical Company. Under reaction temperature of 200~300≧, pressure of 1.6~3.2MPa, LHSV of 3.0~5.0h-1 and H2/oil of 300:1~500:1(v/v), total sulfur removal rate can reach 85%~90%, olefins saturation rate can reach 15%~25%, RON loss is less than 2 units, (R+M)/2(antiknock index) loss is less than 1.5 units and liquid yield is more than 98m%.
Main
operating conditions of OCT-M technology
|
Reaction
temperature/≧ |
200~300 |
|
Reaction
pressure/MPa |
1.6~3.2 |
|
LHSV/h-1 |
3.0~5.0 |
|
H2/oil/(v/v) |
300:1~500:1 |
Typical
results of FCC gasoline selective HDS！pilot plant test
|
Items |
S/m
g〜 g-1 |
Olefins/v% |
RON |
MON |
(R+M)/2
loss |
|
1#
GPC HCN(>90≧) |
2850 |
40.9 |
92.0 |
80.2 |
|
| Hydrotreated
product 1 |
700 |
35.1 |
89.5 |
79.2 |
1.8 |
| Hydrotreated
product 2 |
340 |
28.1 |
87.6 |
78.9 |
2.4 |
| Hydrotreated
product 3 |
207 |
25.0 |
86.0 |
78.4 |
3.9 |
|
2#
GPC HCN(>90≧) |
1260 |
36.6 |
91.4 |
80.2 |
|
|
Hydrotreated
product 1 |
108 |
25.6 |
87.0 |
78.6 |
3.0 |
|
Hydrotreated
product 2 |
55 |
20.2 |
84.7 |
77.4 |
4.8 |
|
Shengli
HCN(>90≧) |
3700 |
46.0 |
87.5 |
77.4 |
|
|
Hydrotreated product |
326 |
27.3 |
83.0 |
75.5 |
3.2 |
|
Shijiazhuang
HCN(>90≧) |
2100 |
35.5 |
86.5 |
77.2 |
|
|
Hydrotreated
product |
180 |
24.8 |
82.6 |
75.0 |
3.2 |
|
Anqing
FCC HCN(>90≧) |
2700 |
38.5 |
89.2 |
78.6 |
|
|
Hydrotreated
product 1 |
200 |
22.1 |
84.6 |
76.6 |
3.3 |
|
Hydrotreated
product 2 |
106 |
17.0 |
82.6 |
76.5 |
4.3 |
Typical
results of blended gasoline from OCT-M process！pilot
plant test
|
Items |
S/m
g〜 g-1 |
S
removal/% |
Olefins/v% |
Olefins
saturation/% |
RON
Loss |
MON
Loss |
(R+M)/2
Loss |
|
1#
GPC feed |
1635 |
|
52.9 |
|
|
|
|
|
Product
1 |
472 |
71.1 |
46.0 |
13.0 |
0.8 |
0.4 |
0.6 |
|
Product
2 |
278 |
83.0 |
44.0 |
16.8 |
1.3 |
0.5 |
0.9 |
|
Product
3 |
192 |
88.3 |
42.1 |
20.4 |
1.7 |
0.6 |
1.2 |
|
2#
GPC feed |
806 |
|
47.3 |
|
|
|
|
|
Product
1 |
134 |
83.4 |
41.0 |
13.3 |
1.3 |
0.5 |
0.9 |
|
Product
2 |
97 |
88.0 |
39.0 |
17.5 |
2.0 |
0.6 |
1.3 |
|
Shengli
feed |
2515 |
|
53.8 |
|
|
|
|
|
Product |
311 |
87.6 |
44.5 |
17.3 |
1.9 |
1.1 |
1.5 |
|
SJZ
feed |
1250 |
|
42.9 |
|
|
|
|
|
Product |
180 |
85.6 |
37.4 |
12.8 |
1.4 |
0.6 |
1.0 |
|
Anqing
feed |
1600 |
|
42.7 |
|
|
|
|
|
Product
1 |
237 |
85.2 |
36.3 |
15.0 |
1.4 |
0.6 |
1.0 |
|
Product
2 |
178 |
88.9 |
35.5 |
16.9 |
1.7 |
0.7 |
1.2 |
Mass-balance
of heavy fraction HDS！Commercial results of GPC
|
Items |
Materials |
Yields
v% |
Quantity |
|
kg/h |
t/d |
t/a |
|
In |
>90≧
HCN |
100 |
26867 |
644.08 |
214936 |
|
Make-up
H2 |
0.88 |
236.43 |
5.67 |
1891.44 |
|
Water
injected |
4.47 |
1200 |
28.8 |
9600 |
|
Steam |
1.12 |
300 |
7.2 |
2400 |
|
Sub-total |
106.47 |
28603.43 |
685.75 |
228827.4 |
|
Out |
S
contained stripped gas |
1.14 |
305.75 |
7.32 |
2446 |
|
Refined
gasoline |
98.86 |
26560.72 |
637.45 |
212485.7 |
|
Sour
water |
5.58 |
1498.66 |
35.27 |
11989.28 |
|
Loss |
0.89 |
238.3 |
5.71 |
1906.4 |
|
Sub-total |
106.47 |
28603.43 |
685.75 |
228827.4 |
Commercial
results of GPC OCT-M unit
|
Items |
Feed |
LCN |
HCN |
Refined
HCN |
Blended
gasoline |
|
Density,
g/cm3 |
0.7288 |
0.6633 |
0.7945 |
0.7904 |
0.7283 |
|
S,
μg/g |
581 |
163 |
730 |
38.3 |
99.0/86.0* |
|
Olefins,
v% |
37.7 |
48.6 |
20.5 |
8.9 |
27.4 |
|
RON |
92.6 |
94.5 |
90.2 |
85.6 |
91.9 |
|
MON |
80.5 |
81.9 |
80.0 |
76.5 |
79.5 |
|
(R+M)/2 |
86.55 |
88.7 |
85.1 |
81.2 |
85.7 |
|
Liquid
yield, m% |
|
|
|
|
99.0 |
*After caustic-scrubbing
Costs of investment and operation
The implementation of OCT-M technology can be based on revamping existed hydrofining plants.
For constructing a new OCT-M plant on a 0.4Mt/a base, capital cost is around USD6.75M, operation costs is around USD3.0/ton feed (including hydrogen cost).
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