• Shift condensate rate
This falls out of the material balances as 2, 378 mols/h (leftover process
steam) = 42.3 Mlb/h or $85 gpm.
• Actual steam/carbon ratio
This also fell out of the calculations as X = 4.53.
• Normalized pressure drop
For normalizing the pressure drop, prior history and a normalization basis
(reference conditions) are required. Here, from prior development work, the
equation for normalization of dP was found to be
dP norm ¼ dP meas  Q feed þ Q steam
ð
Þ norm = Q feed þ Q steam
ð
Þ meas
Â
à 1:6
where:
dP norm = normalized dP at reference conditions
dP meas = measured dP at actual conditions
Q feed = inlet volumetric flow of feed, reference or actual
Q steam = inlet volumetric flow of steam, reference or actual
Here:
dP meas ¼ 315 À 290 psig ¼ 25 psig
Q feed, meas ¼ 6:87 MMscfd
Q steam, meas ¼ 66, 500 lb=h  24 h=day  379:45 scf=18 lbs ! 33:6 MMscfd
Q feed þ Q steam
ð
Þ norm ¼ 51:9 MMscfd ðfor normalization reference caseÞ
So
dP norm ¼ 25 Â 51:9= 6:9 þ 33:6
ð
Þ
½
1:6 ¼ 37 psi
14. From the parameters monitored, we can observe that:
• Depending on how much adjustment was needed to get a good material
balance, flow meter, instrument, or analytical issues may be indicated
that would bear some evaluation.
• The reformer approach to equilibrium is fairly good. Trending the calculated value would provide an indication of deactivation rate.
• The shift converter ATE should also be trended over time for complete
analysis. An ATE of 68
F is a little high and may indicate the shift
converter catalyst has deactivated some or the temperature is not optimum. It could also indicate bad data.
• The PSA recovery efficiency of 83 % is lower than you should expect.
Recovery of at least 85 % should be achievable. This would bear further
investigation.
• The shift condensate rate is informational primarily. It may be needed for
loading evaluation of the degasifier on occasion.
Hydrogen Production and Management for Petroleum Processing
643
This falls out of the material balances as 2, 378 mols/h (leftover process
steam) = 42.3 Mlb/h or $85 gpm.
• Actual steam/carbon ratio
This also fell out of the calculations as X = 4.53.
• Normalized pressure drop
For normalizing the pressure drop, prior history and a normalization basis
(reference conditions) are required. Here, from prior development work, the
equation for normalization of dP was found to be
dP norm ¼ dP meas  Q feed þ Q steam
ð
Þ norm = Q feed þ Q steam
ð
Þ meas
Â
à 1:6
where:
dP norm = normalized dP at reference conditions
dP meas = measured dP at actual conditions
Q feed = inlet volumetric flow of feed, reference or actual
Q steam = inlet volumetric flow of steam, reference or actual
Here:
dP meas ¼ 315 À 290 psig ¼ 25 psig
Q feed, meas ¼ 6:87 MMscfd
Q steam, meas ¼ 66, 500 lb=h  24 h=day  379:45 scf=18 lbs ! 33:6 MMscfd
Q feed þ Q steam
ð
Þ norm ¼ 51:9 MMscfd ðfor normalization reference caseÞ
So
dP norm ¼ 25 Â 51:9= 6:9 þ 33:6
ð
Þ
½
1:6 ¼ 37 psi
14. From the parameters monitored, we can observe that:
• Depending on how much adjustment was needed to get a good material
balance, flow meter, instrument, or analytical issues may be indicated
that would bear some evaluation.
• The reformer approach to equilibrium is fairly good. Trending the calculated value would provide an indication of deactivation rate.
• The shift converter ATE should also be trended over time for complete
analysis. An ATE of 68
F is a little high and may indicate the shift
converter catalyst has deactivated some or the temperature is not optimum. It could also indicate bad data.
• The PSA recovery efficiency of 83 % is lower than you should expect.
Recovery of at least 85 % should be achievable. This would bear further
investigation.
• The shift condensate rate is informational primarily. It may be needed for
loading evaluation of the degasifier on occasion.
Hydrogen Production and Management for Petroleum Processing
643