Hydrocarbon Processing - June 2022 - GP-30

PROCESS OPTIMIZATION
for the regenerator was 307.4 tpd. Moreover,
the total flowrate required was 170
bpd, and the total mass flow required from
MEA was 366.5774 kg/hr. The composition
of sweet gas by mole fraction for
methane was 0.806; for ethane, it was
0.1049. The operating condition for the
rich amine stream was 48.03 kg/cm2
and
the temperature was 39.27°C (102.69°F).
Parametic sensitivity analysis and
simulation modeling using DEA. Treatment
by DEA is shown in TABLE 3. The
H2
S
S and CO2
was 97.47%. The amine
S composition in the sweet gas was
4 ppm. The recovery for removed H2
was 99.33%, while the recovery of both
H2
strength was 32 wt%, and the amount of
regenerated steam required for the regenerator
was 307.4 tpd.
After the trial, it was found that the best
flowrate of DEA to meet specifications
was 310 bpd, and, to meet the concentration
of H2
S in sales gas specifications, the
TABLE 2. MEA unit dashboard
Component
Reboiler duty, kcal/hr
Regenerator steam, tpd
Acid gas loading in
regenerator bottom
Acid gas loading in
regenerator feed
Value
6.495e+006
307.4
1.381e-003
Acid gas loading in acid stream 8.537e+014
0.5495
Regenerator feed
temperature, °C (°F)
Regenerator reflux ratio
(mole basis)
Amine strength, wt%
Amine recirculation rate, bpd
Lean amine temperature,
°C (°F)
Feed gas flowrate, MMft3
H2S composition
in feed gas, ppm
H2S composition
in sweet gas, ppm
H2
S composition
in acid gas, ppm
H2S composition
in regenerator bottom, ppm
H2S composition
in regenerator feed, ppm
Recovery of amine
unit for H2
S, %
Recovery of amine
unit (H2
S and CO2
), %
d
104.4 (219.92)
161.1
32
170
48 (118.4)
12
599.6
4.508e-004
9.603e+004
0.7344
7,083
100
100
30 MAY/JUNE 2022 | GasProcessingNews.com
total mass flowrate required from DEA
was 683.806 kg/hr. In addition, the concentration
(mole fraction) of methane
in the sweet gas stream was 0.8057; for
ethane, it was 0.1049. The operating conditions
of the rich amine included a pressure
of 48.03 kg/cm2
38.98°C (102.16°F).
Parametic sensitivity analysis and
simulation modeling using TEA. Treatment
by TEA is shown in TABLE 4. H2
S
composition in the sweet gas was 0.2037
ppm. The recovery for removed H2
99.97%, while the recovery of both H2
and CO2
S was
S
was 70.29%. The total mass flowrate
of TEA to recover this amount was
2,220 kg/hr. The amine strength was 32
wt%, and the amount of regenerated steam
required for the regenerator was 307.3 tpd.
In addition, the concentration (mole fraction)
of methane in the sweet gas stream
was 0.8042; for ethane, it was 0.1047. The
operating conditions of the rich amine
TABLE 3. DEA unit dashboard
Component
Reboiler duty, kcal/hr
Regenerator steam, tpd
Acid gas loading in
regenerator bottom
Acid gas loading in
regenerator feed
Value
6.494e+006
307.4
2.125e-004
Acid gas loading in acid stream 5.178e+024
0.4927
Regenerator feed
temperature, °C (°F)
Regenerator reflux ratio
(mole basis)
Amine strength, wt%
Amine recirculation rate, bpd
Lean amine temperature,
°C (°F)
Feed gas flowrate, MMft3
H2S composition
in feed gas, ppm
H2S composition
in sweet gas, ppm
H2
S composition
in acid gas, ppm
H2S composition
in regenerator bottom, ppm
H2S composition
in regenerator feed, ppm
Recovery of amine
unit for H2
S, %
Recovery of amine
unit (H2
S and CO2
), %
d
104.4 (219.92)
166.6
32
310
48 (118.4)
12
599.6
4
9.866e+004
0.1783
4,027
99.33
97.47
included a pressure of 48.03 kg/cm2
and
a temperature of 39.22°C (102.6°F). The
total mass flowrate required to remove
acid gas by 70.29% was 1,000 bpd.
Parametic sensitivity analysis and
and a temperature of
simulation modeling using DGA. Treatment
by DGA is shown in TABLE 5. H2
S
composition in the sweet gas was 8.908e002
ppm. The recovery for removed H2
S
was 99.99%, while the recovery of both
H2
S and CO2
was 99.62%. The amine
strength was 32 wt%, and the amount
of regenerated steam required for the regenerator
was 307.3 tpd. The total mass
flowrate required from DGA was 608.73
kg/hr. The concentration (mole fraction)
of methane in the sweet gas stream was
0.8058; for ethane, it was 0.1049. The
operating conditions of the rich amine
included a pressure of 48.03 kg/cm2
and
a temperature of 38.77°C (101.8°F). The
total mass flowrate required to remove
acid gas by 99.62% was 282 bpd.
TABLE 4. TEA unit dashboard
Component
Reboiler duty, kcal/hr
Regenerator steam, tpd
Acid gas loading in
regenerator bottom
Acid gas loading in
regenerator feed
Value
6.492e+006
307.3
3.012e-005
Acid gas loading in acid stream 8.086e+027
0.1553
Regenerator feed
temperature, °C (°F)
Regenerator reflux ratio
(mole basis)
Amine strength, wt%
Amine recirculation rate, bpd
Lean amine temperature,
°C (°F)
Feed gas flowrate, MMft3
H2S composition
in feed gas, ppm
H2S composition
in sweet gas, ppm
H2
S composition
in acid gas, ppm
H2S composition
in regenerator bottom, ppm
H2S composition
in regenerator feed, ppm
Recovery of amine
unit for H2
S, %
Recovery of amine
unit (H2
S and CO2
), %
d
104.4 (219.92)
225.1
32
1,000
48 (118.4)
12
599.6
0.2037
1.344e+005
5.208e-007
4,027
99.33
97.47
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Hydrocarbon Processing - June 2022

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