## Oxygen Supply Design Optimization

## Main.OxygenStorage History

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The tank pressure is subject to the constraint:

The maximimum design tank pressure has a lower bound as given by the following constraint:

**Acknowledgements**

Thanks to Adam Martin for providing the problem statement and the solution.

The two design variables for this system are the maximum storage tank pressure (`p` in psia) and the oxygen production rate (`F` in tons/hour). The given constants are the low oxygen demand rate (`D_0`) at 2.4 tons/hour, the high oxygen demand rate (`D_1`) at 37 tons/hour, the gas constant (`R`) at 670.6 `ft^{3}` lb/`in^2`/(HP-hr), temperature (`T`) at 530 degrees Rankine, the compressibility factor 0.98 (`z`), unit conversion factor (`k_1`) at 14005.8, compressor efficiency (`k_2`) at 0.75, and the oxygen delivery pressure (`p_0`) at 200 psia.

The two design variables for this system are the maximum storage tank pressure (`p` in psia) and the oxygen production rate (`F` in tons/hour). The given constants are the low oxygen demand rate (`D_0`) at 2.4 tons/hour, the high oxygen demand rate (`D_1`) at 37 tons/hour, the gas constant (`R`) at 670.6 `ft^{3}` psia/(HP-hr), temperature (`T`) at 530 degrees Rankine, the compressibility factor 0.98 (`z`), unit conversion factor (`k_1`) at 14005.8, compressor efficiency (`k_2`) at 0.75, and the oxygen delivery pressure (`p_0`) at 200 psia.

#### Cost Functions

#### Annual Cost Function

#### Constraints

#### Full Problem Statement

#### Assignment

The two design variables for this system are the maximum storage tank pressure (`p` in psia) and the oxygen production rate (`F` in tons/hour). The given constants are the low oxygen demand rate (`D_0`) at 2.4 tons/hour, the high oxygen demand rate (`D_1`) at 37 tons/hour, the gas constant (`R`) at 670.6 `({{ft}^{3} (lb/in^2)}/{HP - hr})`, temperature (`T`) at 530 degrees Rankine, the compressibility factor 0.98 (`z`), unit conversion factor (`k_1`) at 14005.8, compressor efficiency (`k_2`) at 0.75, and the oxygen delivery pressure (`p_0`) at 200 psia.

The two design variables for this system are the maximum storage tank pressure (`p` in psia) and the oxygen production rate (`F` in tons/hour). The given constants are the low oxygen demand rate (`D_0`) at 2.4 tons/hour, the high oxygen demand rate (`D_1`) at 37 tons/hour, the gas constant (`R`) at 670.6 `ft^{3}` lb/`in^2`/(HP-hr), temperature (`T`) at 530 degrees Rankine, the compressibility factor 0.98 (`z`), unit conversion factor (`k_1`) at 14005.8, compressor efficiency (`k_2`) at 0.75, and the oxygen delivery pressure (`p_0`) at 200 psia.

The two design variables for this system are the maximum storage tank pressure (`p` in psia) and the oxygen production rate (`F` in tons/hour). The given constants are the low oxygen demand rate (`D_0`) at 2.4 tons/hour, the high oxygen demand rate (`D_1`) at 37 tons/hour, the gas constant (`R`) at 670.6 (`{ft^3 psia}/{(HP - HR)})`), temperature (`T`) at 530 degrees Rankine, the compressibility factor 0.98 (`z`), unit conversion factor (`k_1`) at 14005.8, compressor efficiency (`k_2`) at 0.75, and the oxygen delivery pressure (`p_0`) at 200 psia.

The two design variables for this system are the maximum storage tank pressure (`p` in psia) and the oxygen production rate (`F` in tons/hour). The given constants are the low oxygen demand rate (`D_0`) at 2.4 tons/hour, the high oxygen demand rate (`D_1`) at 37 tons/hour, the gas constant (`R`) at 670.6 `({{ft}^{3} (lb/in^2)}/{HP - hr})`, temperature (`T`) at 530 degrees Rankine, the compressibility factor 0.98 (`z`), unit conversion factor (`k_1`) at 14005.8, compressor efficiency (`k_2`) at 0.75, and the oxygen delivery pressure (`p_0`) at 200 psia.

The annual cost (`AC`) of the BOF system is found using the following equation. Here `d` is an annual cost factor for the compressor and storage tank and `N` is the number of cycles in one year of operation.

The annual cost (`AC`) of the BOF system is found using the following equation. The parameter `d` is an annual cost factor for the compressor and storage tank and `N` is the number of cycles in one year of operation.

There are four cost elements. $C_1$ is the oxygen plant annual cost `C_1 = a_1 + a_2F`, $C_2$ is the capital cost of the storage vessel `C_2 = s_1 \, s_2 \, V^{s_3}`, $C_3$ is the capital cost of the compressor `C_3 = 0.2 \, b_1 \, b_2 \, H^{b_3}`, and $C_4$ is the compressor power cost `C_4 = 0.001 \, b_4 \, t_1 \, H`. In these equations $a_1$, $a_2$, $s_1$, $s_2$, $s_3$, $b_1$, $b_2$, $b_3$, $b_4$ are cost parameters.

There are four cost elements. `C_1` is the oxygen plant annual cost `C_1 = a_1 + a_2F`, `C_2` is the capital cost of the storage vessel `C_2 = s_1 \, s_2 \, V^{s_3}`, `C_3` is the capital cost of the compressor `C_3 = 0.2 \, b_1 \, b_2 \, H^{b_3}`, and `C_4` is the compressor power cost `C_4 = 0.001 \, b_4 \, t_1 \, H`. In these equations `a_1`, `a_2`, `s_1`, `s_2`, `s_3`, `b_1`, `b_2`, `b_3`, `b_4` are cost parameters.

`s_2` | 660 | $(ft^3)^{-b_3}$ |

`s_2` | 660 | `(ft^3)^{-b_3}` |

The maximum amount of oxygen stored (`I_{max}`) in the tank during the cycle can be calculated as:

The maximum amount of oxygen stored (`I_{max}`) in the tank during the cycle is calculated as:

$$H = \frac{I_{max}}{t_1} \frac{RT}{k_1k_2} \ln{ \frac{p}{p_0}}$$

The maximum tank pressure is subject to the constraint:

$$H = \frac{I_{max}}{t_1} \frac{RT}{k_1k_2} \ln{(\frac{p}{p_0})}$$

The tank pressure is subject to the constraint:

p = m.Var() #Maximum tank pressure (psia)

p = m.Var() #Tank pressure (psia)

(:title Oxygen Supply Design Optimization:) (:keywords nonlinear, optimization, engineering optimization, manufacturing, engineering design, gekko, tutorial, python:) (:description Engineering design of an oxygen supply system to stay within constraints and meet an optimal criteria. Optimization principles are used to design the system.:)

The operation of a Basic Oxygen Furnace (BOF) is based on cycles. Each cycle consists of a low oxygen demand interval in which raw materials are introduced to the furnace, and a high oxygen demand interval in which the raw material is processed. The low demand interval is 0.4 hours, and the high demand interval (`t_1`) is 0.6 hours, giving a total cycle time (`t_2`) of 1 hour. Due to equipment limitations, the oxygen production rate (`F`) is held constant throughout the cycle. Any excess oxygen produced during the low demand period is compressed and stored, to be withdrawn as needed during the high demand period. The objective of this problem is to design an oxygen-supply and storage system that meets the oxygen demand of the furnace over the entire cycle while minimizing cost. The following figure shows the BOF system.

The two design variables for this system are the maximum storage tank pressure (`p` in psia) and the oxygen production rate (`F` in tons/hour). The given constants are the low oxygen demand rate (`D_0`) at 2.4 tons/hour, the high oxygen demand rate (`D_1`) at 37 tons/hour, the gas constant (`R`) at 670.6 (`{ft^3 psia}/{(HP - HR)})`), temperature (`T`) at 530 degrees Rankine, the compressibility factor 0.98 (`z`), unit conversion factor (`k_1`) at 14005.8, compressor efficiency (`k_2`) at 0.75, and the oxygen delivery pressure (`p_0`) at 200 psia.

These values are used to calculate the compressor design capacity (`H`) and the storage tank design capacity (`V`). These intermediate values are then used to calculate the total cost of the system.

#### Cost Functions

The annual cost (`AC`) of the BOF system is found using the following equation. Here `d` is an annual cost factor for the compressor and storage tank and `N` is the number of cycles in one year of operation.

$$AC = C_1 + (C_2 + C_3)\,d + N\,C_4$$

There are four cost elements. $C_1$ is the oxygen plant annual cost `C_1 = a_1 + a_2F`, $C_2$ is the capital cost of the storage vessel `C_2 = s_1 \, s_2 \, V^{s_3}`, $C_3$ is the capital cost of the compressor `C_3 = 0.2 \, b_1 \, b_2 \, H^{b_3}`, and $C_4$ is the compressor power cost `C_4 = 0.001 \, b_4 \, t_1 \, H`. In these equations $a_1$, $a_2$, $s_1$, $s_2$, $s_3$, $b_1$, $b_2$, $b_3$, $b_4$ are cost parameters.

**Table 1: Cost parameters for the oxygen supply and storage system**

Parameter | Value | Units |

`a_1` | 60.9 | dollars/hour |

`a_2` | 5.83 | dollars/hour |

`b_1` | 2.5e-5 | dollars/hour |

`b_2` | 680 | `HP^{-c_3}` |

`b_3` | 0.85 | dimensionless |

`b_4` | 6.0e-3 | dollars/(HP-HR) |

`s_1` | 3.0e-5 | dollars/hour |

`s_2` | 660 | $(ft^3)^{-b_3}$ |

`s_3` | 0.9 | dimensionless |

`d` | 5 | dimensionless |

`N` | 8000 | dimensionless |

The maximum amount of oxygen stored (`I_{max}`) in the tank during the cycle can be calculated as:

$$I_{max} = (D_1 - F)\,(t_2 - t_1)$$

The compressor design capacity is given by:

$$H = \frac{I_{max}}{t_1} \frac{RT}{k_1k_2} \ln{ \frac{p}{p_0}}$$

The maximum tank pressure is subject to the constraint:

$$p >= p_0 + 1$$

To meet the required oxygen demand the production rate must meet the following constraint:

$$F >= \frac{D_0 \, t_1 + D_1 \, (t_2 - t_1)}{t_2}$$

Full Oxygen Supply Design Assignment (PDF)

Turn in a report with the following sections:

- Title Page with Summary. The Summary should be short (less than 50 words), and give the main optimization results.
- Procedure: Give a brief description of your model. You are welcome to refer to the assignment which should be in the Appendix. Also include:
- A table with the analysis variables, design variables, analysis functions and design functions.

- Results: Briefly describe the results of optimization (values). Also include:
- A table showing the optimum values of variables and functions, indicating binding constraints and/or variables at bounds (highlighted)
- A table giving the various starting points which were tried along with the optimal objective values reached from that point.

- Discussion of Results: Briefly discuss the optimum and design space around the optimum. Do you feel this is a global optimum? Also include and briefly discuss:
- A “zoomed out” contour plot showing the design space (both feasible and infeasible) for diameter and thickness, with the feasible region shaded and optimum marked.
- A “zoomed in” contour plot of the design space (mostly feasible space) for diameter and thickness, with the feasible region shaded and optimum marked.

- Appendix:
- Listing of your model with all variables and equations
- Solver output with details of the convergence to the optimal values

Any output from the software is to be integrated into the report (either physically or electronically pasted) as given in the sections above. Tables and figures should all have explanatory captions. Do not just staple pages of output to your assignment: all raw output is to have notations made on it. For graphs, you are to shade the feasible region and mark the optimum point. For tables of design values, you are to indicate, with arrows and comments, any variables at bounds, any binding constraints, the objective, etc. (You need to show that you understand the meaning of the output you have included.)

**References**

- A Ravindran, Gintaras Victor Reklaitis, and Kenneth Martin Ragsdell. Engineering optimization: methods and applications. John Wiley & Sons, 2006.
- Frank C. Jen, C. Carl Pegels, and Terrence M. Dupuis. Optimal capacities of production facilities. Management Science, 14(10):B573–B580, 1968.

**Solution Help**

See GEKKO documentation and additional example problems.

(:source lang=python:) from gekko import GEKKO

m = GEKKO()

- Model Oxygen Supply
- Constants

R = 670.6 #gas law (cubic feet-psia/(HP - HR)) T = 530 #Temperature (degrees Rankine) z = 0.98 #Compressibility factor () M = 15.999 #Molecular weight (u) k_1 = 14005.8 #unit conversion factor

- cycle parameters

N = 8000 #Number of cycles per year D_0 = 2.4 #Low demand rate of O_2 (tons/hr) D_1 = 37 #High demand rate of O_2 (tons/hr) t_1 = 0.6 #time interval of high demand rate t_2 = 1 #time interval of one cycle of low and high demand rate

- cost parameters

a_1 = 60.9 a_2 = 5.83 b_1 = 2.5e-5 b_2 = 680 b_3 = 0.85 b_4 = 6.0e-3 #cost of power s_1 = 3.0e-5 s_2 = 374 s_3 = 0.9 d = 5 #annual cost factor

- physical parameters

p_0 = 200 #O_2 delivery pressure k_2 = 0.75 #Compressor efficiency

- Variables
- Independent variables

F = m.Var() #Production rate(tons/hr) p = m.Var() #Maximum tank pressure (psia) annual_cost = m.Var() #Objective.

- Intermediates

I_max = m.Intermediate((D_1 - F)*(t_2 - t_1)) V = m.Intermediate((I_max/M)*(R*T/p)*z) H = m.Intermediate((I_max/t_1)*(R*T/(k_1*k_2))*m.log(p/p_0))

- Oxygen plant annual cost

C_1 = m.Intermediate(a_1 + a_2*F)

- Capital cost of storage vessels

C_2 = m.Intermediate(s_1*s_2*V**s_3)

- Capital cost of compressors

C_3 = m.Intermediate(0.2*b_1*b_2*H**b_3)

- Compressor power cost

C_4 = m.Intermediate(0.001*b_4*t_1*H)

- Equations

m.Equations([

annual_cost == C_1 + d*(C_2 + C_3) + N*C_4, F >= (D_0*t_1 + D_1*(t_2 - t_1))/t_2, p >= p_0 + 1 ])

- Objective

m.Obj(annual_cost)

- Solve

m.solve()

print("Optimal annual cost:" , str(annual_cost[0])) print("Optimal production rate:" , str(F[0])) print("Optimal maximum tank pressure:" , str(p[0])) (:sourceend:)

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