Optimal Design of a Two-Stage Membrane System for Hydrogen Separation in Refining Processes
Abstract
:1. Introduction
2. Process Description
- The way in which the driving force for permeation is created in each membrane stage, i.e., the solution will indicate if the driving force is created by (a) employing compression without applying vacuum, or (b) applying vacuum in the permeate streams without employing compression, or (c) combining both compression and vacuum.
- The inclusion or not of the expansion turbine for power recovery.
- The inclusion or not of (one or more) recycle streams.
- The optimal values of operation pressure, temperature, composition, and flow rate of each process stream.
- The optimal sizes of the process units (membrane areas, heat transfer areas, power capacity of compressors and vacuum pumps).
3. Process Modeling
3.1. Main Model Assumptions
- All the mixture components can permeate through the membrane.
- The operating pressure does not affect the component permeability.
- No pressure drop is considered in the retentate and permeate sides.
- The feed and retentate streams are at the same pressure.
- Plug flow pattern is considered at both sides of the membrane unit.
- Isothermal condition is assumed within the membrane module.
- Fick’s first law is used.
3.2. Mathematical Model
3.2.1. Mass Balances
3.2.2. Power Requirement
3.2.3. Energy Balances and Transfer Areas of Heat Exchangers
3.2.4. Connecting Constraints
3.2.5. Performance Variables
3.2.6. Cost Model
4. Results and Discussion
4.1. Comparison of Optimal and Sub-Optimal Solutions
4.2. Sensitivity Analysis
4.2.1. Sensitivity of the Optimal Solution to the H2 Product Purity Level
4.2.2. Sensitivity of the Optimal Solution to the H2 Recovery Level
5. Conclusions
Author Contributions
Funding
Acknowledgments
Conflicts of Interest
Nomenclature
AMS# | membrane area required in the membrane stage MS#, m2. |
annCAPEX | annualized capital expenditures, M$·year−1. |
CAPEX | capital expenditures, M$. |
CRF | capital recovery factor, year−1. |
CRM | raw material and utility cost, M$·year−1 |
cruCW | specific cost of the cooling water, M$·kg−1. |
cruEP | specific cost of the electricity, M$·kW−1. |
cruMR | specific cost of the membrane replacement, M$·m−2. |
F0 | feed flow rate, kmol·s−1. |
FMS# | feed flow rate in the membrane stage MS#, kmol·s−1. |
IMS# | investment for membrane area of the stage MS#, M$. |
IHEX# | investment for the heat exchanger HEX#, M$. |
IVP# | investment for the vacuum pump VP#, M$. |
IC# | investment for the compressor C#, M$. |
OPEX | operating expenditures, M$·year−1. |
pH | high operating pressure (retentate side), MPa. |
pLMS# | operating pressure in the permeate side of the membrane stage MS#, MPa. |
PMS# | permeate flow rate obtained in the membrane stage MS#, kmol·s−1. |
RMS# | retentate flow rate obtained in the membrane stage MS#, kmol·s−1. |
TAC | total annual cost, M$·year−1. |
T0 | feed temperature, K. |
Tout C# | outlet temperature from the compressor C# associated with the membrane stage MS#, K. |
TMS# | operating temperature in the membrane stage MS#, K. |
Tout HEX# | outlet temperature from the heat exchanger HEX#, K. |
WC# | power required by the compressor C# associated with the membrane stage MS#, MW. |
WVP# | power required by the vacuum pump VP# in the membrane stage MS#, MW. |
WEXP | power recovered in the expander EXP, MW. |
xi,0 | mole fraction of component i in the feed stream, dimensionless. |
xMS#,i | inlet composition of the component i in the membrane stage MS#, dimensionless. |
xMS#,i,j | mole fraction of the component i in the retentate stream of the membrane stage MS# at the discretization point j, dimensionless. |
xMS#,R,i | mole fraction of the component i in the retentate stream leaving the membrane stage MS#, dimensionless. |
yMS#,i | mole fraction of the component i in the permeate stream leaving the membrane stage MS#, dimensionless. |
yMS1,i,j | mole fraction of the component i in the permeate stream of the membrane stage MS# at the discretization point j, dimensionless. |
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Parameter | Value |
---|---|
Feed specification | |
Flow rate, kmol·h−1 | 100 |
Temperature, K | 313.15 |
Pressure, kPa | 101.32 |
Composition (mole fraction) | |
CO2 | 0.04 |
CO | 0.16 |
H2 | 0.18 |
N2 | 0.62 |
Membrane material (Polymer) | |
Permeance, mole·m−2·s−1·MPa−1) | |
CO2 | 8.444 × 10−3 |
CO | 7.457 × 10−4 |
H2 | 2.871 × 10−2 |
N2 | 4.078 × 10−4 |
Optimal Sol. OPT | Sub-Optimal Sol. SUBOPT1 | Sub-Optimal Sol. SUBOPT2 | |
---|---|---|---|
TAC (M$·year−1) | 1.764 | 2.038 | 2.182 |
OPEX (M$·year−1) | 1.095 | 1.262 | 1.272 |
annCAPEX (M$·year−1) | 0.669 | 0.776 | 0.911 |
CINV (M$) | 1.431 | 1.661 | 1.948 |
C1 | 0.694 | 0.916 | 0.642 |
C2 | 0.316 | 0.480 | 0.299 |
AMS1 | 0.269 | 0.214 | 0.344 |
VP1 | 0.077 | 0.0 | 0.080 |
AMS2 | 0.034 | 0.015 | 0.040 |
HEX1 | 0.020 | 0.022 | 0.020 |
HEX2 | 0.011 | 0.013 | 0.010 |
HEX3 | 0.010 | 0.0 | 0.010 |
VP2 | 0.0 | 0.0 | 7.96 × 10−3 |
EXP | 0.0 | 0.0 | 0.494 |
CRM (M$·year−1) | 0.155 | 0.211 | 0.094 |
EP | 0.141 | 0.198 | 0.077 |
MR | 0.011 | 8.61 × 10−3 | 0.014 |
CW | 2.79 × 10−3 | 3.90 × 10−3 | 2.76 × 10−3 |
H2 Product Purity | |||||
---|---|---|---|---|---|
Dev. (%) | 0.89 | 0.90 | 0.91 | Dev. (%) | |
Cost item | |||||
TAC (M$·year−1) | −1.32 | 1.741 | 1.764 | 1.802 | +2.11 |
OPEX (M$·year−1) | −1.30 | 1.081 | 1.095 | 1.118 | +2.04 |
annCAPEX (M$·year−1) | −1.36 | 0.660 | 0.669 | 0.684 | +2.24 |
CINV (M$) | −1.36 | 1.411 | 1.431 | 1.463 | +2.24 |
IC1 | −1.24 | 0.685 | 0.694 | 0.705 | +1.63 |
IC2 | −4.72 | 0.302 | 0.316 | 0.337 | +6.46 |
IMA_MS1 | +1.48 | 0.273 | 0.269 | 0.266 | −1.00 |
IVP1 | −5.80 | 7.22 × 10−2 | 7.67 × 10−2 | 8.28 × 10−2 | +8.04 |
IMA_MS2 | +15.83 | 3.94 × 10−2 | 3.40 × 10−2 | 2.96 × 10−2 | −12.88 |
IHEX1 | −0.49 | 2.02 × 10−2 | 2.03 × 10−2 | 2.04 × 10−2 | +0.54 |
IHEX2 | −4.11 | 1.02 × 10−2 | 1.07 × 10−2 | 1.13 × 10−2 | +5.79 |
IHEX3 | −3.74 | 1.00 × 10−2 | 1.04 × 10−2 | 1.09 × 10−2 | +4.99 |
CRM (M$·year−1) | −3.18 | 0.150 | 0.155 | 0.162 | +4.52 |
CE | −3.67 | 0.136 | 0.141 | 0.148 | +5.06 |
CMR | +3.07 | 1.175 × 10−2 | 1.140 × 10−2 | 1.113 × 10−2 | −2.36 |
CCW | −4.30 | 2.67 × 10−3 | 2.79 × 10−3 | 2.95 × 10−3 | +5.73 |
Design item | |||||
pH (MPa) | −2.84 | 0.581 | 0.598 | 0.621 | +3.84 |
TMA (m2) | +3.10 | 5878.9 | 5701.7 | 5567.3 | −2.35 |
TW (MW) | −3.69 | 0.287 | 0.298 | 0.313 | +5.03 |
H2 Recovery | |||||
---|---|---|---|---|---|
Dev. (%) | 89% | 90% | 91% | Dev. (%) | |
Cost Item | |||||
TAC (M$·year−1) | −1.49 | 1.738 | 1.764 | 1.793 | +1.64 |
OPEX (M$·year−1) | −1.40 | 1.080 | 1.095 | 1.112 | +1.54 |
annCAPEX (M$·year−1) | −1.64 | 0.658 | 0.669 | 0.681 | +1.80 |
CINV (M$) | −1.64 | 1.407 | 1.431 | 1.457 | +1.80 |
IC1 | −1.34 | 0.684 | 0.694 | 0.703 | +1.42 |
IC2 | −3.22 | 0.306 | 0.316 | 0.328 | +3.58 |
IMA_MS1 | −0.88 | 0.266 | 0.268 | 0.271 | +0.95 |
IVP1 | −3.17 | 7.48 × 10−2 | 7.67 × 10−2 | 7.94 × 10−2 | +3.57 |
IMA_MS2 | +3.59 | 3.52 × 10−2 | 3.40 × 10−2 | 3.27 × 10−2 | −3.76 |
IHEX1 | −0.54 | 2.02 × 10−2 | 2.03 × 10−2 | 2.04 × 10−2 | +0.44 |
IHEX2 | −2.24 | 10.45 × 10−3 | 10.70 × 10−3 | 10.95 × 10−3 | +2.43 |
IHEX3 | −1.72 | 1.02 × 10−2 | 1.04 × 10−2 | 1.06 × 10−2 | +1.82 |
CRM (M$·year−1) | −2.74 | 0.151 | 0.155 | 0.160 | +3.02 |
CE | −2.92 | 0.137 | 0.141 | 0.145 | +3.23 |
CMR | −0.35 | 1.136 × 10−2 | 1.140 × 10−2 | 1.145 × 10−2 | +0.43 |
CCW | −2.86 | 2.71 × 10−3 | 2.79 × 10−3 | 2.88 × 10−3 | +3.22 |
Design item | |||||
pH (MPa) | −3.01 | 0.580 | 0.598 | 0.618 | +3.34 |
TMA (m2) | −0.36 | 5680.9 | 5701.7 | 5725.2 | +0.41 |
TW (MW) | −3.02 | 0.289 | 0.298 | 0.307 | +3.02 |
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Share and Cite
Arias, A.M.; Mores, P.L.; Scenna, N.J.; Caballero, J.A.; Mussati, S.F.; Mussati, M.C. Optimal Design of a Two-Stage Membrane System for Hydrogen Separation in Refining Processes. Processes 2018, 6, 208. https://doi.org/10.3390/pr6110208
Arias AM, Mores PL, Scenna NJ, Caballero JA, Mussati SF, Mussati MC. Optimal Design of a Two-Stage Membrane System for Hydrogen Separation in Refining Processes. Processes. 2018; 6(11):208. https://doi.org/10.3390/pr6110208
Chicago/Turabian StyleArias, Ana M., Patricia L. Mores, Nicolás J. Scenna, José A. Caballero, Sergio F. Mussati, and Miguel C. Mussati. 2018. "Optimal Design of a Two-Stage Membrane System for Hydrogen Separation in Refining Processes" Processes 6, no. 11: 208. https://doi.org/10.3390/pr6110208
APA StyleArias, A. M., Mores, P. L., Scenna, N. J., Caballero, J. A., Mussati, S. F., & Mussati, M. C. (2018). Optimal Design of a Two-Stage Membrane System for Hydrogen Separation in Refining Processes. Processes, 6(11), 208. https://doi.org/10.3390/pr6110208