Poto?nik P. (Ed.) Natural Gas
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The effect of H
2
S on hydrogen and carbon black production from sour natural gas 171
reaction that begins at lower temperatures than that of H
2
S. Also, Fig. 6 depicts that
temperature drops precipitously with increasing flow rate of feed gas due to the
endothermic nature of both CH
4
and H
2
S decompositions.
Fig. 3. Comparison of the predicted reactor outlet temperature with the experimental data
Fig. 4. Comparison of the predicted carbon black yield with the experimental data
1100
1300
1500
1700
1900
2100
0 0,5 1 1,5 2 2,5 3 3,5 4
Temprature(k)
Feedstock Mass Flow Rate (1000*kg/s)
Exp. [4 ]
Pre. [this study]
0
10
20
30
40
0,0 1,0 2,0 3,0 4,0 5,0 6,0
Carbon Black yield [%]
Equivalence Ratio
Exp. [4 ]
Pre. [This study]
Fig. 5. Contour of species mass fractions and temperature (K)
Natural Gas172
Fig. 6. Effect of feedstock flow rate on calculated outlet temperature
Figs. 7 and 8 show the effect of feed gas flow rate and reactor outlet temperature on CH
4
and
H
2
S conversions given by [Huang & T-Raissi, 2008]:
100
]CH[
]CH[]CH[
conversionCH
0
0
4
44
4
,
100
]SH[
]SH[]SH[
conversionSH
0
0
2
22
2
where
04
]CH[
and
02
]SH[
denote the initial (input) concentration of CH
4
and H
2
S,
respectively.
]CH[
4
and
]SH[
2
are equilibrium concentration of CH
4
and H
2
S at reactor
outlet, respectively. Fig. 7 depicts that the H
2
S conversion drops sharply with increased feed
gas flow rate, which can be attributed to the endothermic nature of H
2
S and CH
4
decomposition reactions. For higher values of feed gas flow rate
)s/kg002.0(
CH
4
conversion decreases with increased feed gas flow rate due to the endothermicity of CH
4
thermolysis. The major factor influencing CH
4
and H
2
S conversions appears to be
temperature. Fig. 8 shows that CH
4
conversion reaches 100% at temperatures above
K1100
. Because CH
4
decomposition reaction is mildly endothermic, the temperature must
be above
K850
for the reaction to proceed at a reasonable rate. This is in accordance with
the results of Huang and T-Raissi (2008). At any temperature, H
2
S conversion is less than
that of CH
4
, especially at those below
K1300
wherein H
2
S conversion is less than 5%. For
higher values of reactor temperature
)K1300(
, H
2
S conversion increases sharply with
reaction temperature. As the reaction of H
2
S decomposition is endothermic, the temperature
must be above
K1500
for the reaction to proceed at rapid rates.
1100
1300
1500
1700
1900
2100
0 1 2 3 4 5 6
Temperature(K)
Feedstock Mass Flow Rate (1000*kg/s)
Without H2S
With 10% H2S (mass)
.
Fig. 7. Effect of feedstock mass flow rate on H
2
S and CH
4
conversions
Fig. 8. Effect of reactor outlet temperature on H
2
S and CH
4
conversions
Figs. 9 shows the effect of feedstock flow rate on CH
4
, carbon black, soot and CO mass
fractions at the furnace outlet. It can be seen that for lower values of feed gas flow rates, the
very high temperature pre-combustor effluent (see Fig. 6) causes the feedstock methane to
convert to CO rather than carbon. For higher values of feedstock flow rate, the formation of
carbon black increases, and due to the resulting lower temperatures, the mass fraction of CO
and soot decreases. This is so because the soot model strongly depends on the reaction
temperature. Fig. 10 shows the effect of feedstock flow rate on H
2
and carbon black yields at
70
75
80
85
90
95
100
0
20
40
60
80
100
800 1200 1600 2000
CH4 conversion (%)
H2S conversion(%)
Temperature (K)
H2S
CH4
The effect of H
2
S on hydrogen and carbon black production from sour natural gas 173
Fig. 6. Effect of feedstock flow rate on calculated outlet temperature
Figs. 7 and 8 show the effect of feed gas flow rate and reactor outlet temperature on CH
4
and
H
2
S conversions given by [Huang & T-Raissi, 2008]:
100
]CH[
]CH[]CH[
conversionCH
0
0
4
44
4
,
100
]SH[
]SH[]SH[
conversionSH
0
0
2
22
2
where
04
]CH[
and
02
]SH[
denote the initial (input) concentration of CH
4
and H
2
S,
respectively.
]CH[
4
and
]SH[
2
are equilibrium concentration of CH
4
and H
2
S at reactor
outlet, respectively. Fig. 7 depicts that the H
2
S conversion drops sharply with increased feed
gas flow rate, which can be attributed to the endothermic nature of H
2
S and CH
4
decomposition reactions. For higher values of feed gas flow rate
)s/kg002.0(
CH
4
conversion decreases with increased feed gas flow rate due to the endothermicity of CH
4
thermolysis. The major factor influencing CH
4
and H
2
S conversions appears to be
temperature. Fig. 8 shows that CH
4
conversion reaches 100% at temperatures above
K1100
. Because CH
4
decomposition reaction is mildly endothermic, the temperature must
be above
K850
for the reaction to proceed at a reasonable rate. This is in accordance with
the results of Huang and T-Raissi (2008). At any temperature, H
2
S conversion is less than
that of CH
4
, especially at those below
K1300
wherein H
2
S conversion is less than 5%. For
higher values of reactor temperature
)K1300(
, H
2
S conversion increases sharply with
reaction temperature. As the reaction of H
2
S decomposition is endothermic, the temperature
must be above
K1500
for the reaction to proceed at rapid rates.
1100
1300
1500
1700
1900
2100
0 1 2 3 4 5 6
Temperature(K)
Feedstock Mass Flow Rate (1000*kg/s)
Without H2S
With 10% H2S (mass)
.
Fig. 7. Effect of feedstock mass flow rate on H
2
S and CH
4
conversions
Fig. 8. Effect of reactor outlet temperature on H
2
S and CH
4
conversions
Figs. 9 shows the effect of feedstock flow rate on CH
4
, carbon black, soot and CO mass
fractions at the furnace outlet. It can be seen that for lower values of feed gas flow rates, the
very high temperature pre-combustor effluent (see Fig. 6) causes the feedstock methane to
convert to CO rather than carbon. For higher values of feedstock flow rate, the formation of
carbon black increases, and due to the resulting lower temperatures, the mass fraction of CO
and soot decreases. This is so because the soot model strongly depends on the reaction
temperature. Fig. 10 shows the effect of feedstock flow rate on H
2
and carbon black yields at
70
75
80
85
90
95
100
0
20
40
60
80
100
800 1200 1600 2000
CH4 conversion (%)
H2S conversion(%)
Temperature (K)
H2S
CH4
Natural Gas174
the furnace outlet. It can be seen that the yield of H
2
increases with increased feed gas flow
rate until it reaches a maximum value, and then drops with further increase in the flow rate.
For higher values of feedstock flow rate, the yield of carbon black increases and due to
reduction in CH4 conversion (see Fig. 7) the yield of hydrogen decreases.
Fig. 9. Effect of feedstock flow rate on CH
4
, CO, carbon black, and soot mass fractions
Fig. 10. Effect of feedstock mass flow rate on H
2
and C(S) productions
0
2
4
6
8
10
12
14
16
18
0
1
2
3
4
5
6
0 1 2 3 4 5 6
Mass Fraction of CO(%)
Mass fraction of soot, CH4 &
carbon black (%)
Feedstock Mass Flow Rate (1000*kg/s)
Soot
Carbon black
CO
CH4
0
20
40
60
80
100
0 1 2 3 4 5 6
Yields of C(S) , H
2
(%)
Feedstock Mass Flow Rate (1000*kg/s)
H
2
C(s)
Fig. 11 depicts the yield of sulfur (due to H
2
S decomposition) and SO
2
(due to H
2
S
combustion) as a function of feedstock flow rate at the outlet of the furnace. S
2
and SO
2
yields are defined as [Huang & T-Raissi, 2008]:
100*
]SH[
]S[2
(%)S
02
2
2
, 100*
]SH[
]SO[
(%)SO
02
2
2
.
where
]S[
2
and
]SO[
2
denote the equilibrium molar concentrations of
2
S
and
2
SO
,
respectively. The figure reveals that for low values of feedstock flow rate
)s/kg002.0(
that
result in high reaction temperatures (see Fig. 3)
SH
2
converts mostly to
2
S
and
2
SO
. It can
be seen that for higher values of feedstock flow rate, yield of
2
S
and
2
SO
are quite low.
This is due to reduced of
SH
2
conversion (see Fig. 7). Figs. 12 and 13 depict the effects of
feedstock mass flow rate and temperature on the yield of COS and
2
CS
, respectively, as
defined by:
100*
]SH[
]COS[
(%)COS
02
,
100*
]CH[
]CS[
(%)CS
04
2
2
where
]COS[
and
]CS[
2
denote the equilibrium molar concentration of COS and CS
2
,
respectively [Huang & T-Raissi, 2008]. Fig. 12 shows that COS and
2
CS
yields increase
with increased feedstock flow rate until they reach a peak, and then drop with further
increase in feed gas flow rate. Figs. 12 reveals that yield of
2
CS
is always low
%)0007.0(
.
This is in accord with results of Huang &T-Raissi (2008) and Towler & Lynn (1996).
Fig. 11. Effect of feedstock mass flow rate on
2
S
and
2
SO
0
10
20
30
40
50
60
70
0 1 2 3
S2 and SO2 yields(%)
Feedstock mass flow rate (1000*kg/s)
SO2
S2
The effect of H
2
S on hydrogen and carbon black production from sour natural gas 175
the furnace outlet. It can be seen that the yield of H
2
increases with increased feed gas flow
rate until it reaches a maximum value, and then drops with further increase in the flow rate.
For higher values of feedstock flow rate, the yield of carbon black increases and due to
reduction in CH4 conversion (see Fig. 7) the yield of hydrogen decreases.
Fig. 9. Effect of feedstock flow rate on CH
4
, CO, carbon black, and soot mass fractions
Fig. 10. Effect of feedstock mass flow rate on H
2
and C(S) productions
0
2
4
6
8
10
12
14
16
18
0
1
2
3
4
5
6
0 1 2 3 4 5 6
Mass Fraction of CO(%)
Mass fraction of soot, CH4 &
carbon black (%)
Feedstock Mass Flow Rate (1000*kg/s)
Soot
Carbon black
CO
CH4
0
20
40
60
80
100
0 1 2 3 4 5 6
Yields of C(S) , H
2
(%)
Feedstock Mass Flow Rate (1000*kg/s)
H
2
C(s)
Fig. 11 depicts the yield of sulfur (due to H
2
S decomposition) and SO
2
(due to H
2
S
combustion) as a function of feedstock flow rate at the outlet of the furnace. S
2
and SO
2
yields are defined as [Huang & T-Raissi, 2008]:
100*
]SH[
]S[2
(%)S
02
2
2
, 100*
]SH[
]SO[
(%)SO
02
2
2
.
where
]S[
2
and
]SO[
2
denote the equilibrium molar concentrations of
2
S
and
2
SO
,
respectively. The figure reveals that for low values of feedstock flow rate
)s/kg002.0(
that
result in high reaction temperatures (see Fig. 3)
SH
2
converts mostly to
2
S
and
2
SO
. It can
be seen that for higher values of feedstock flow rate, yield of
2
S
and
2
SO
are quite low.
This is due to reduced of
SH
2
conversion (see Fig. 7). Figs. 12 and 13 depict the effects of
feedstock mass flow rate and temperature on the yield of COS and
2
CS
, respectively, as
defined by:
100*
]SH[
]COS[
(%)COS
02
,
100*
]CH[
]CS[
(%)CS
04
2
2
where
]COS[
and
]CS[
2
denote the equilibrium molar concentration of COS and CS
2
,
respectively [Huang & T-Raissi, 2008]. Fig. 12 shows that COS and
2
CS
yields increase
with increased feedstock flow rate until they reach a peak, and then drop with further
increase in feed gas flow rate. Figs. 12 reveals that yield of
2
CS
is always low
%)0007.0(
.
This is in accord with results of Huang &T-Raissi (2008) and Towler & Lynn (1996).
Fig. 11. Effect of feedstock mass flow rate on
2
S
and
2
SO
0
10
20
30
40
50
60
70
0 1 2 3
S2 and SO2 yields(%)
Feedstock mass flow rate (1000*kg/s)
SO2
S2
Natural Gas176
Fig. 12. Effect of feedstock mass flow rate on COS and CS
2
yields
6.2 Type 2: pyrolysis by inert hot gases
In the case of Type 2, the inert hot gas (argon) flow rate introduced into the pre-combustor is
3
3 10 kg / s
with pressure of 1 bar and the temperature varying from 600 K to 1800 K. The
feedstock sour natural gas feed rate is
3 3
19 10 m / s
with H
2
S/CH
4
molar ratio varying
from 0 to 4 and the temperature of 300 K. As the reactions of CH
4
and
H
2
S decomposition
are endothermic, in order to avoid the reduction of inert gas temperature some thermal
elements have been utilized.
Figs. 13 and 14 illustrate the effects of feedstock H
2
S/CH
4
ratio and reaction temperature on CH
4
and H
2
S conversions. Results show that the major factor influencing CH
4
and H
2
S conversions is
temperature. As the temperature increases, CH
4
conversion also increases to reach 100% at
temperatures above 1100 K for H
2
S/CH
4
feed ratio ranging from 0 to 4. Since the endothermic
reaction of CH
4
conversion occurs at lower temperatures compared with H
2
S conversion, the
reactor temperature is significantly affected by CH
4
molar ratio in feedstock. Based on these
results it can be concluded that as the reaction temperature increases up to about 1100 K,
methane pyrolysis is the dominant reaction that controls reactor temperature. H
2
S decomposition
is the limiting step in the H
2
S-methane reformation process (Reaction 3) as it proceeds by the
sequential reaction involving H
2
S pyrolysis to form sulfur diatomic gas (S
2
) (Reaction 2), followed
by S
2
reaction with CH
4
to produce carbon disulfide (CS
2
) and H
2
. Fig. 15 depicts that H
2
production increases by increasing molar ratio of CH
4
(decreasing H
2
S/CH
4
ratio) in feedstock
and temperature. The rate of hydrogen production from pyrolysis of methane is much more than
that of hydrogen sulfide. Therefore, any reduction in H
2
S/CH
4
feed ratio, for constant feedstock
mass flow rate, leads to significant increase in hydrogen production rate.
Figs. 16 and 17 depict the yields of carbon and sulfur as a function of H
2
S /CH
4
feed ratio
and reaction temperature. Fig. 16 shows that carbon yield increases with increasing
-0,001
0,001
0,003
0,005
0,007
0,009
0
0,5
1
1,5
2
2,5
3
3,5
0 1 2 3 4 5 6
CS2 yield(%)
COS yield (%)
Feedstock Mass Flow Rate (1000*kg/s)
COS
CS2
temperature until the yield reaches a maximum value (at about 1000K), and then drops
with further increase in the temperature for H
2
S/CH
4
ratios more than zero.
Fig. 13. The effect of reaction temperature and feedstock H
2
S/CH
4
ratio on CH
4
conversion
for constant feedstock mass flow rate in the case of Type 2
Fig. 14. The effect of reaction temperature and feedstock H
2
S/CH
4
ratio on H
2
S conversion
for constant feedstock mass flow rate in the case of Type 2
0
0,2
0,4
0,6
0,8
1
600 900 1200 1500 1800
CH
4
Conversion
Temprature(k)
H2S/CH4= 0:1
01:04
02:03
03:02
04:02
06:02
08:02
H
2
S/CH
4
0
0,2
0,4
0,6
0,8
1
600 900 1200 1500 1800
H2S Conversion
Temprature(k)
H2S:CH4=01:04
02:03
03:02
04:02
06:02
08:02
H
2
S/CH
4
The effect of H
2
S on hydrogen and carbon black production from sour natural gas 177
Fig. 12. Effect of feedstock mass flow rate on COS and CS
2
yields
6.2 Type 2: pyrolysis by inert hot gases
In the case of Type 2, the inert hot gas (argon) flow rate introduced into the pre-combustor is
3
3 10 kg / s
with pressure of 1 bar and the temperature varying from 600 K to 1800 K. The
feedstock sour natural gas feed rate is
3 3
19 10 m / s
with H
2
S/CH
4
molar ratio varying
from 0 to 4 and the temperature of 300 K. As the reactions of CH
4
and
H
2
S decomposition
are endothermic, in order to avoid the reduction of inert gas temperature some thermal
elements have been utilized.
Figs. 13 and 14 illustrate the effects of feedstock H
2
S/CH
4
ratio and reaction temperature on CH
4
and H
2
S conversions. Results show that the major factor influencing CH
4
and H
2
S conversions is
temperature. As the temperature increases, CH
4
conversion also increases to reach 100% at
temperatures above 1100 K for H
2
S/CH
4
feed ratio ranging from 0 to 4. Since the endothermic
reaction of CH
4
conversion occurs at lower temperatures compared with H
2
S conversion, the
reactor temperature is significantly affected by CH
4
molar ratio in feedstock. Based on these
results it can be concluded that as the reaction temperature increases up to about 1100 K,
methane pyrolysis is the dominant reaction that controls reactor temperature. H
2
S decomposition
is the limiting step in the H
2
S-methane reformation process (Reaction 3) as it proceeds by the
sequential reaction involving H
2
S pyrolysis to form sulfur diatomic gas (S
2
) (Reaction 2), followed
by S
2
reaction with CH
4
to produce carbon disulfide (CS
2
) and H
2
. Fig. 15 depicts that H
2
production increases by increasing molar ratio of CH
4
(decreasing H
2
S/CH
4
ratio) in feedstock
and temperature. The rate of hydrogen production from pyrolysis of methane is much more than
that of hydrogen sulfide. Therefore, any reduction in H
2
S/CH
4
feed ratio, for constant feedstock
mass flow rate, leads to significant increase in hydrogen production rate.
Figs. 16 and 17 depict the yields of carbon and sulfur as a function of H
2
S /CH
4
feed ratio
and reaction temperature. Fig. 16 shows that carbon yield increases with increasing
-0,001
0,001
0,003
0,005
0,007
0,009
0
0,5
1
1,5
2
2,5
3
3,5
0 1 2 3 4 5 6
CS2 yield(%)
COS yield (%)
Feedstock Mass Flow Rate (1000*kg/s)
COS
CS2
temperature until the yield reaches a maximum value (at about 1000K), and then drops
with further increase in the temperature for H
2
S/CH
4
ratios more than zero.
Fig. 13. The effect of reaction temperature and feedstock H
2
S/CH
4
ratio on CH
4
conversion
for constant feedstock mass flow rate in the case of Type 2
Fig. 14. The effect of reaction temperature and feedstock H
2
S/CH
4
ratio on H
2
S conversion
for constant feedstock mass flow rate in the case of Type 2
0
0,2
0,4
0,6
0,8
1
600 900 1200 1500 1800
CH
4
Conversion
Temprature(k)
H2S/CH4= 0:1
01:04
02:03
03:02
04:02
06:02
08:02
H
2
S/CH
4
0
0,2
0,4
0,6
0,8
1
600 900 1200 1500 1800
H2S Conversion
Temprature(k)
H2S:CH4=01:04
02:03
03:02
04:02
06:02
08:02
H
2
S/CH
4
Natural Gas178
Fi
g
fe
e
Fi
g
m
a
g
. 15. Yield of H
e
dstock mass flo
w
g
. 16. The effects
a
ss flow rate
2
as a function
o
w
rate
of temperature
o
f reaction temp
e
and H
2
S/CH
4
r
a
e
rature and H
2
S
/
a
tio on C(s)
y
ield
/
CH
4
ratio for c
o
d
for constant fee
o
nstant
dstock
In
de
m
e
co
n
ra
t
se
c
y
i
e
de
lo
w
ar
e
Fi
g
fe
e
7.
T
h
m
e
he
temperatures
l
composition. Bu
t
e
thane and h
y
d
r
n
sumed b
y
CS
2
t
io or the reacti
o
c
tion, h
y
dro
g
en
s
e
ld for temperat
u
pend not onl
y
o
n
w
er than 1000K,
e
in accordance
w
g
. 17. The effect
s
e
dstock mass flo
w
Conclusions
h
e production o
f
e
thane (CH
4
) an
d
at. Based on the
p
The ma
j
or fac
t
At temperatu
r
At an
y
tempe
below 1300K
For lower v
a
consequentl
y
,
rates
y
ield of
hi
g
her feed
ga
l
ower than 10
0
t
in temperature
s
r
o
g
en sulfide,
a
production (Fi
g
.
o
n temperature,
s
ulfide requires
h
u
res lower than
n
the temperatu
r
the
y
ield of car
b
w
ith results of H
u
s
of reaction te
m
w
rate
f
h
y
dro
g
en and
d
h
y
dro
g
en sulfi
d
p
rese
n
ted results
,
t
or influencin
g
C
r
es above 1100
K
rature, H
2
S conv
for which H
2
S c
o
a
lues of feedst
o
the
y
ield of car
b
carbon black in
a
s flow rates.
0
0K, h
y
dro
g
en
s
more than 100
0
a
nd formed soli
d
18). Fi
g
. 17 de
p
S
2
y
ield increas
e
h
i
g
h temperatur
e
1000
◦
K is ne
g
li
g
r
e, but also on t
h
b
on disulfide (CS
2
u
an
g
and T-Raiss
i
m
perature and
H
carbon black fr
o
d
e (H
2
S) has be
e
,
the followin
g
c
o
H
4
and H
2
S con
v
K
, CH
4
conversio
n
ersion is less tha
n
o
nversion is less
t
o
ck flow rate,
C
b
on black is low.
F
creases to a ma
x
and carbon a
r
0
K h
y
dro
g
en is
p
d
carbon from
p
icts that b
y
eith
e
e
s. As explaine
d
e
s to be decomp
g
ible. As shown
h
e H
2
S/CH
4
fee
d
2
) approaches ze
r
i
(2008).
H
2
S/CH
4
ratio o
n
o
m sub-qualit
y
n
e
n anal
y
zed for
t
o
nclusions ma
y
b
v
ersions is reacto
r
n
is complete.
n
that of CH
4
, es
p
t
han 5%.
C
H
4
is converte
F
or hi
g
her value
s
x
imum value be
f
r
e produced b
y
p
roduced from
b
CH
4
decomposi
t
e
r increasin
g
H
2
S
d
in chemical re
a
osed. Conseque
n
in Fi
g
.18 , CS
2
d
ratio. In tempe
r
r
o (Fi
g
. 7). These
r
n
S
2
y
ield for c
o
n
atural
g
as con
t
t
wo t
y
pes of sup
e drawn:
r
temperature.
p
eciall
y
at temp
e
d to mostl
y
C
O
s
of feed
g
as ma
s
f
ore droppin
g
at
y
CH
4
b
oth o
f
t
ion is
S
/CH
4
a
ctions
n
tl
y
, S
2
2
yield
r
atures
r
esults
o
nstant
t
ainin
g
pl
y
in
g
e
rature
O
and
s
s flow
much
The effect of H
2
S on hydrogen and carbon black production from sour natural gas 179
Fi
g
fe
e
Fi
g
m
a
g
. 15. Yield of H
e
dstock mass flo
w
g
. 16. The effects
a
ss flow rate
2
as a function
o
w
rate
of temperature
o
f reaction temp
e
and H
2
S/CH
4
r
a
e
rature and H
2
S
/
a
tio on C(s)
y
ield
/
CH
4
ratio for c
o
d
for constant fee
o
nstant
dstock
In
de
m
e
co
n
ra
t
se
c
y
i
e
de
lo
w
ar
e
Fi
g
fe
e
7.
T
h
m
e
he
temperatures
l
composition. Bu
t
e
thane and h
y
d
r
n
sumed b
y
CS
2
t
io or the reacti
o
c
tion, h
y
dro
g
en
s
e
ld for temperat
u
pend not onl
y
o
n
w
er than 1000K,
e
in accordance
w
g
. 17. The effect
s
e
dstock mass flo
w
Conclusions
h
e production o
f
e
thane (CH
4
) an
d
at. Based on the
p
The ma
j
or fac
t
At temperatu
r
At an
y
tempe
below 1300K
For lower v
a
consequentl
y
,
rates yield of
hi
g
her feed
ga
l
ower than 10
0
t
in temperature
s
r
o
g
en sulfide,
a
production (Fi
g
.
o
n temperature,
s
ulfide requires
h
u
res lower than
n
the temperatu
r
the
y
ield of car
b
w
ith results of H
u
s
of reaction te
m
w
rate
f
h
y
dro
g
en and
d
h
y
dro
g
en sulfi
d
p
rese
n
ted results
,
t
or influencin
g
C
r
es above 1100
K
rature, H
2
S conv
for which H
2
S c
o
a
lues of feedst
o
the
y
ield of car
b
carbon black in
a
s flow rates.
0
0K, hydrogen
s
more than 100
0
a
nd formed soli
d
18). Fi
g
. 17 de
p
S
2
y
ield increas
e
h
i
g
h temperatur
e
1000
◦
K is ne
g
li
g
r
e, but also on t
h
b
on disulfide (CS
2
u
an
g
and T-Raiss
i
m
perature and
H
carbon black fr
o
d
e (H
2
S) has be
e
,
the followin
g
c
o
H
4
and H
2
S con
v
K
, CH
4
conversio
n
ersion is less tha
n
o
nversion is less
t
o
ck flow rate,
C
b
on black is low.
F
creases to a ma
x
and carbon a
r
0
K h
y
dro
g
en is
p
d
carbon from
p
icts that b
y
eith
e
e
s. As explaine
d
e
s to be decomp
g
ible. As shown
h
e H
2
S/CH
4
fee
d
2
) approaches ze
r
i
(2008).
H
2
S/CH
4
ratio o
n
o
m sub-qualit
y
n
e
n anal
y
zed for
t
o
nclusions ma
y
b
v
ersions is reacto
r
n
is complete.
n
that of CH
4
, es
p
t
han 5%.
C
H
4
is converte
F
or hi
g
her value
s
x
imum value be
f
r
e produced b
y
p
roduced from
b
CH
4
decomposi
t
e
r increasin
g
H
2
S
d
in chemical re
a
osed. Conseque
n
in Fi
g
.18 , CS
2
d
ratio. In tempe
r
r
o (Fi
g
. 7). These
r
n
S
2
y
ield for c
o
n
atural
g
as con
t
t
wo t
y
pes of sup
e drawn:
r
temperature.
p
eciall
y
at temp
e
d to mostl
y
C
O
s
of feed
g
as ma
s
f
ore dropping at
y
CH
4
b
oth o
f
t
ion is
S
/CH
4
a
ctions
n
tl
y
, S
2
2
yield
r
atures
r
esults
o
nstant
t
ainin
g
pl
y
in
g
e
rature
O
and
s
s flow
much
Natural Gas180
Fi
g
fe
e
8.
A
b
A
b
A
b
The yield of
h
flow rate unti
l
For tempera
t
temperature.
Since CH
4
co
n
the reactor te
m
The carbon
y
further increa
s
CS2 and COS
y
ield in inert
g
g
. 18. The effect
s
e
dstock mass flo
w
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