Hydrocarbon Processing - April 2021 - 42
Clean Fuels
drocracker are more than three times
higher than the capital costs for implementation of the proprietary upgrading
process unit of the same capacity. Outside battery limit integration costs are
also significantly lower for a proprietary
upgrading process unit. On a per-barrel
cause little or no disruption to
existing refinery infrastructure.
Commercially, the proprietary upgrading process is a lower-priced alternative to hydrocracking. Capital costs
for estimated inside battery limits for
implementation of an ebullated-bed hy-
Lean amine
Makeup H2
Amine
scrubber
Recycle gas
compressor
Reactor
system
Rich amine
Heater
To fuel gas
Water
Wild naphtha
ISO 8217 HSFO
Stabilizer
Hot
separator
Cold
separator
ISO 8217 proprietary
VLSFO product
FIG. 1. Process flow diagram of the proprietary upgrading process.
operating cost basis, the proprietary upgrading process unit is about one-fourth
the operating costs of an ebullated-bed
hydrocracker. The proprietary upgrading process is much less operationally
complex and is safer than residue upgrading alternatives.
In addition to the benefits outlined,
a modular proprietary upgrading process unit allows much faster entry into
the market, with the lowest need for
integration and disruption to existing
infrastructure at either a refinery or marine terminal. A modular version of the
proprietary upgrading process can be
fully operational at a greenfield site in
less than 2 yr from the date of placing an
order-or even sooner, if located inside
an existing refinery, which is half of the
schedule for a comparable ebullated-bed
hydrocracker or coker. Beyond price
and speed-to-market considerations,
both coking and hydrocracking produce
some amount of low-value residual material that must be sold into the market
at a value lower than the feedstock and
TABLE 1. Comparison of the proprietary fuel
RMG 380 ISO 8217
specification
RMG 380*
Marine gasoil
80/20 blend
to 0.5% sulfur**
Proprietary
VLSFOb
991 max.
990.3
870.1
891.7
950.2
Yield
Density at 15°C (59°F)
Metric tons (t)
1
1
1
1
Barrels at 15°C (59°F)
6.36
7.24
7.07
6.63
Volume in m3 at 15°C (59°F)
1.01
1.15
1.12
1.05
2.5
< 0.1
0.5
0.45
Specific energy
Sulfur content, % m/m
0.5 max.
Ash content, % m/m
0.09
< 0.01
0.03
< 0.01
Gross specific energy, Btu/gal
152,000
142,000
144,000
150,000
Net specific energy, Btu/gal
143,000
133,000
135,000
142,000
870
852
-
831
824
-
-
40
-
-
Carbon residue, wt%
18 max.
12.18
0
2.6
6.59
Aluminum and silicon, mg/kg
60 max.
52
0
10
<1
Calculated carbon aromaticity index (CCAI)
Cetane index
Carbon and metals
Vanadium, mg/kg
35 max.
151
0
30
20
Sodium, mg/kg
100 max.
40
0
8
<1
Acid number, mg KOG/g
2.5 max.
0.53
0.15
0.23
< 0.05
Kinematic viscosity at 50°C
380 max.
369.7
2.5
4.4
120
Pour point, °C
30 max.
-12
-2
-4
-18
Flash point, °C
60 min.
101
66
68.7
110
* RMG 380 is a blend of refinery streams. It is now salable as HSFO.
** Blend of RMG 380 and sufficient gasoil to meet the 0.5% sulfur requirement
42
APRIL 2021 | HydrocarbonProcessing.com
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Hydrocarbon Processing - April 2021
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