4. Unit operation results#

4.1. A note on design and modeling#

BioSTEAM includes a wide range of unit operation models and cost correlations adapted from design textbooks and literature [1-5]. Essential unit operations such as pumps, heat exchangers, flash vessels, mixer-settlers, and distillation columns are some of the most rigorously modeled and designed. Design requirements for these essential units are calculated based on design specifications such as operating temperature and pressure, feed conditions, construction material, and degree of separation. These design requirements include, but are not limited to, the heat-transfer area of heat exchangers, the size and thickness of pressure vessels, and number of stages in a distillation column. Other unit operation models are modeled as splitters (i.e., a specified fraction of each component entering a unit is separated), and the purchase price is estimated using size factor correlations that are ultimately a function of material flow rates. BioSTEAM chooses purchase price correlations and construction factors based on the design specifications and requirements for each unit operation. For detailed documentation and examples of each unit operation, visit the units subpackage documentation.

4.2. Distillation columns#

In the following example, BioSTEAM’s distillation column is used to highlight key details here on where do unit operations store results:

[1]:

from biosteam import Stream, settings
import biosteam as bst
bst.nbtutorial()

# First set the property package
settings.set_thermo(['Water', 'Ethanol'])

# Create the feed at the bubble point
feed = Stream('feed', Water=1.08e+03, Ethanol=586)
bp = feed.bubble_point_at_P()
feed.T = bp.T # Feed at bubble point temperature

# Create a distillation column and simulate
# Use BinaryDistillation for 2-components
# For 3+ components, use ShortcutColumn
# For rigorous distillation with side draws and feeds at multiple stages, use MESHDistillation
D1 = bst.BinaryDistillation(
    'D1', ins=feed,
    outs=('distillate', 'bottoms_product'),
    LHK=('Ethanol', 'Water'), # Light and heavy keys
    y_top=0.79, # Light key composition at the distillate
    x_bot=0.001, # Light key composition at the bottoms product
    k=1.25, # Ratio of actual reflux over minimum reflux
    is_divided=True, # Whether the rectifying and stripping sections are divided
)
D1.diagram(format='png')
D1.show()
../_images/tutorial_Unit_operation_results_5_0.png 
BinaryDistillation: D1
ins...
[0] feed
    phase: 'l', T: 354.28 K, P: 101325 Pa
    flow (kmol/hr): Water    1.08e+03
                    Ethanol  586
outs...
[0] distillate
    phase: 'l', T: 298.15 K, P: 101325 Pa
    flow: 0
[1] bottoms_product
    phase: 'l', T: 298.15 K, P: 101325 Pa
    flow: 0

Before simulating a distillation column, no results are available, streams are empty, and the components are initialized but empty as well:

[2]:

D1.design_results

[2]:

{}

[3]:

D1.purchase_costs

[3]:

{}

[4]:

D1.heat_utilities

[4]:

[]

[5]:

D1.power_utility

PowerUtility:
consumption: 0 kW
production: 0 kW
power: 0 kW
cost: 0 USD/hr

All unit operations have the design_results, purchase_costs, heat_utilities, and power_utility attributes. The heat_utilities attribute is a list of HeatUtility objects and the power_utility attribute is a PowerUtility object. Unit operations may also have attributes and components specific to that unit operation. Let’s look at the condenser within the diagram:

[6]:

D1.condenser.diagram()
D1.condenser.show()

HXutility: condenser
ins...
[0] vapor  from  BinaryDistillation-D1
    phase: 'g', T: 298.15 K, P: 101325 Pa
    flow: 0
outs...
[0] to  RefluxDrum-reflux_drum
    phases: ('g', 'l'), T: 298.15 K, P: 101325 Pa
     flow: 0

After simulation, the unit operation along with its components will calculate all design results, purchase costs, and utilities:

[7]:

D1.simulate()
D1.diagram(format='png')
D1.show(T='degC', P='atm', composition=True)
../_images/tutorial_Unit_operation_results_14_0.png 
BinaryDistillation: D1
ins...
[0] feed
    phase: 'l', T: 81.125 degC, P: 1 atm
    composition (%): Water    64.8
                     Ethanol  35.2
                     -------  1.67e+03 kmol/hr
outs...
[0] distillate
    phase: 'g', T: 78.484 degC, P: 1 atm
    composition (%): Water    21
                     Ethanol  79
                     -------  741 kmol/hr
[1] bottoms_product
    phase: 'l', T: 99.64 degC, P: 1 atm
    composition (%): Water    99.9
                     Ethanol  0.1
                     -------  925 kmol/hr

[8]:

D1.condenser.show()

HXutility: condenser
ins...
[0] vapor  from  BinaryDistillation-D1
    phase: 'g', T: 351.72 K, P: 101325 Pa
    flow (kmol/hr): Water    329
                    Ethanol  1.13e+03
outs...
[0] to  RefluxDrum-reflux_drum
    phases: ('g', 'l'), T: 351.63 K, P: 101325 Pa
    flow (kmol/hr): (g) Water    156
                        Ethanol  585
                    (l) Water    173
                        Ethanol  540

[9]:

D1.design_results

[9]:

{'Theoretical feed stage': 26,
 'Theoretical stages': 31,
 'Minimum reflux': 0.7708367097030262,
 'Reflux': 0.9635458871287828,
 'Rectifier stages': 45.0,
 'Stripper stages': 9.0,
 'Rectifier height': 78.940416,
 'Stripper height': 25.804416,
 'Rectifier diameter': 9.960477527218737,
 'Stripper diameter': 7.836628484724038,
 'Rectifier wall thickness': 0.4375,
 'Stripper wall thickness': 0.375,
 'Rectifier weight': 41837.555210317725,
 'Stripper weight': 12158.19021210372}

[10]:

D1.purchase_costs

[10]:

{'Rectifier trays': 90190.76854619542,
 'Stripper trays': 19469.07052587847,
 'Rectifier tower': 154203.6774309562,
 'Stripper platform and ladders': 48571.69910583489,
 'Stripper tower': 69659.22647677979,
 'Rectifier platform and ladders': 17028.366373260913,
 'Condenser - Floating head': 65778.41245145093,
 'Reflux drum - Vertical pressure vessel': 40913.03779781813,
 'Reflux drum - Platform and ladders': 10650.872732593733,
 'Pump - Pump': 4526.2951512221225,
 'Pump - Motor': 440.800042798914,
 'Reboiler - Floating head': 65109.26213301633}

[11]:

D1.heat_utilities

[11]:

[<cooling_water: -2.84e+07 kJ/hr, 1.94e+04 kmol/hr, 9.45 USD/hr>,
 <low_pressure_steam: 6.26e+07 kJ/hr, 1.62e+03 kmol/hr, 385 USD/hr>]

[12]:

D1.power_utility

PowerUtility:
consumption: 2.49 kW
production: 0 kW
power: 2.49 kW
cost: 0.195 USD/hr

The results() method can conviniently present all these results:

[13]:

D1.results()

[13]:
Divided Distillation Column Units D1
Electricity Power kW 2.49
Cost USD/hr 0.195
Cooling water Duty kJ/hr -2.84e+07
Flow kmol/hr 1.94e+04
Cost USD/hr 9.45
Low pressure steam Duty kJ/hr 6.26e+07
Flow kmol/hr 1.62e+03
Cost USD/hr 385
Design Theoretical feed stage 26
Theoretical stages 31
Minimum reflux Ratio 0.771
Reflux Ratio 0.964
Rectifier stages 45
Stripper stages 9
Rectifier height ft 78.9
Stripper height ft 25.8
Rectifier diameter ft 9.96
Stripper diameter ft 7.84
Rectifier wall thickness in 0.438
Stripper wall thickness in 0.375
Rectifier weight lb 4.18e+04
Stripper weight lb 1.22e+04
Purchase cost Rectifier trays USD 9.02e+04
Stripper trays USD 1.95e+04
Rectifier tower USD 1.54e+05
Stripper platform and ladders USD 4.86e+04
Stripper tower USD 6.97e+04
Rectifier platform and ladders USD 1.7e+04
Condenser - Floating head USD 6.58e+04
Reflux drum - Vertical pressure vessel USD 4.09e+04
Reflux drum - Platform and ladders USD 1.07e+04
Pump - Pump USD 4.53e+03
Pump - Motor USD 441
Reboiler - Floating head USD 6.51e+04
Total purchase cost USD 5.87e+05
Utility cost USD/hr 395

Note that the units for the design results are in the _units dictionary:

[14]:

D1._units

[14]:

{'Minimum reflux': 'Ratio',
 'Reflux': 'Ratio',
 'Rectifier height': 'ft',
 'Rectifier diameter': 'ft',
 'Rectifier wall thickness': 'in',
 'Rectifier weight': 'lb',
 'Stripper height': 'ft',
 'Stripper diameter': 'ft',
 'Stripper wall thickness': 'in',
 'Stripper weight': 'lb',
 'Height': 'ft',
 'Diameter': 'ft',
 'Wall thickness': 'in',
 'Weight': 'lb'}

It is also possible to retrieve design results in another set of units:

[15]:

rectifier_height = D1.get_design_result('Rectifier height', 'meter')
round(rectifier_height)

[15]:

24

For completeness, here are the rest of the results:

[16]:

D1.condenser.diagram()
D1.condenser.show()

HXutility: condenser
ins...
[0] vapor  from  BinaryDistillation-D1
    phase: 'g', T: 351.72 K, P: 101325 Pa
    flow (kmol/hr): Water    329
                    Ethanol  1.13e+03
outs...
[0] to  RefluxDrum-reflux_drum
    phases: ('g', 'l'), T: 351.63 K, P: 101325 Pa
    flow (kmol/hr): (g) Water    156
                        Ethanol  585
                    (l) Water    173
                        Ethanol  540

[17]:

D1.reboiler.diagram()
D1.reboiler.show()

HXutility: reboiler
ins...
[0] from  Pump-pump
    phase: 'l', T: 370.63 K, P: 101325 Pa
    flow (kmol/hr): Water    2.36e+03
                    Ethanol  19.6
outs...
[0] to  PhaseSplitter-bottoms_split
    phases: ('g', 'l'), T: 372.79 K, P: 101325 Pa
    flow (kmol/hr): (g) Water    1.44e+03
                        Ethanol  18.7
                    (l) Water    924
                        Ethanol  0.925

Unit operations may also have special methods that you may find useful:

[18]:

from matplotlib import pyplot as plt
D1.plot_stages()
plt.show()
../_images/tutorial_Unit_operation_results_30_0.png

4.3. References#

  1. Seider, W. D.; Lewin, D. R.; Seader, J. D.; Widagdo, S.; Gani, R.; Ng, M. K. Cost Accounting and Capital Cost Estimation. In Product and Process Design Principles; Wiley, 2017; pp 426−485.

  2. Svrcek, W. Y.; Monnery, W. D. Design Two-Phase Separators Within the Right Limits. In Chemical Engineering Progress (CEP); The American Institute of Chemical Engineers, 1993; pp 53−60.

  3. Apostolakou, A. A.; Kookos, I. K.; Marazioti, C.; Angelopoulos, K. C. Techno-Economic Analysis of a Biodiesel Production Process from Vegetable Oils. Fuel Process. Technol. 2009, 90, 1023−1031.

  4. Green, D. W. Distillation. In Perry’s Chemical Engineers’ Handbook, 9 ed.; McGraw-Hill Education, 2018.

  5. Duss, M.; Taylor, R. Predict Distillation Tray Efficiency. Chem. Eng. Prog. 2018, 24−30.