# Practical Energy Retrofit of Heat Exchanger Network Not Containing Utility Path

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## Abstract

**:**

## 1. Introduction

## 2. Materials and Methods

**X**changer Suite® (Heat Transfer Research, Inc. (HTRI), Navasota, Texas, TX, USA) from Heat Transfer Research, Inc. (further HTRI) was used to the DD stage performing [28]. The algorithm of the whole method is presented in Figure 3.

- Stating desired retrofit targets and collecting input data about the process and its existing Heat Exchanger Network (process streams data extraction from a process scheme, further identification of hot and cold process streams, current hot and cold utility heat load, and existing heat exchanger performance and heat duties). Depicting the current HEN using the Grid Diagram (GD).
- The EMAT (exchanger minimum approach temperature) value determination. It is a minimum allowable temperature approach of process media in the newly designed HEs creating new Utility Paths. The EMAT value evaluation is dependent on the existing HEN parameters and is discussed by Zhu and Asante [29].

- All thermodynamically feasible Utility Paths, thus the potential locations for the new HE insertion, are drawn to the GD of the current non-standard HEN. The obtained representation of feasible Utility Paths in GD is called the Retrofit Superstructure Grid Diagram (RSGD), which is a platform for the most efficient Utility Path identification. Only feasible matches are included in RSGD, which simplifies its structure and excludes unrealizable HEN modifications.
- Every realizable Utility Path contained in RSGD is verified from the Maximum Heat Recovery Potential (R
_{max}) point of view using a linear programming (LP) model to the Network Pinch diagnosis. Specifically, there is an applied so-called Basic LP Model P1 for Identification of the Network Pinch published by Zhu and Asante [29]. This linear model allows finding R_{max}(i.e., a suitable location for the new HE insertion) considering a specified EMAT value. Use of the linear model ensures finding the so-called global optimum solution, i.e., the optimal location for a new HE insertion is obtained, which is the main objective of this part of the developed method. Linear model implementation is also less difficult due to its simplicity in comparison with using the non-linear model. For the LP Model P1 application, any software enabling numerical programming can be used. In this work, the educational version of software Maple 2018 (Maplesoft, Waterloo, ON, Canada) [30] from the company Maplesoft is used, where the optimization package Simplex provides an appropriate numerical tool. The linear model consists of the process and thermal characteristics of the streams (as a flowrate and specific heat capacity), the heat balance of existing heat exchangers, and the EMAT value. The objective function is the maximization of the R_{max}value described above. - When all the potential Utility Paths from the RSGD are assessed by the LP model, the obtained results are sorted to the so-called Retrofit Identification Table (RIT) from the most beneficial to the least beneficial Utility Path in terms of achievable R
_{max}. The main advantage of using RIT is the simultaneous profitability evaluation of each potential Utility Path, the location for a new HE insertion, and its heat duty. - The most beneficial Utility Path found in RIT (therefore with highest R
_{max}) is suitable for the new HE insertion. These results obtained in the RI stage are input data for the following (detail design) stage of the developed retrofit method. - In case that the results of RI do not satisfy the required reduction of utility loads to the desired level, the RI stage is applied repeatedly, taking the most beneficial Utility Path from the previous search as a basis of the HEN topology for the next search, for finding the next most beneficial Utility Path (see Figure 3).

- The new HEs are of the same type, design, and size as adjacent exchangers operating with the same fluids. This ensures the purchase and maintenance cost minimization and the interchangeability of the exchangers and their parts.
- In case that the new HE does not reach the desired heat duty, try to switch the position of the working fluids in the exchanger, if possible.
- If the desired heat duty is still not reached, the common and cheap technology for heat transfer enhancement may be implemented with respect to the set constraints (allowed pressure drop, etc.). Thus, the required HE performance can be accomplished with minimal investment cost.
- Verify the final retrofit design and consult it with the client, respectively the process operator.

## 3. Case Study

#### Description of the Studied Process

## 4. Results and Discussion

#### 4.1. Preparation Procedure to the HEN Retrofit Design

- (i)
- The requirements received by the plant owner imply that the retrofit of the hydrogenation process could be defined as the energy retrofit, which aims to reduce the hot utility demand (i.e., the process furnace fuel consumption) by at least 30% with minimal investment costs, while the process media pressure drop can exceed maximum 30 kPa for each.
- (ii)
- Within the process input data collection, the hot and cold streams, taking part in the process heat exchange, were identified, via Section 3. All key equipment was analyzed, including the heat exchangers forming the current HEN, whose main characteristics are summarized in Table 1. According to the collected data, the Grid Diagram was further generated and is illustrated in Figure 5. As it is observed in GD, the current HEN does not contain any Utility Path; therefore, it is defined as the non-standard HEN, and thus the developed retrofit method can be applied.
- (iii)
- The EMAT value determination adequate for the existing HEs retrofit as well as for the potential newly designed HEs was carried out according to the instruction provided in [29]. Individual EMAT values of the existing heat exchangers in the studied process range between approximately 88 and 109 °C. Taking into account a very high oversizing of the existing exchangers (see Table 1), the EMAT = 40 °C has been assessed as a practical and operationally easy to achieve value for the existing heat exchangers and also for any new units placed to the HEN of studied process. Additionally, the feasibility of meeting the required hot utility saving was verified by performing the standard targeting procedure (Klemeš et al. [31]). The maximum feasible hot utility saving for the obtained EMAT value is 52.3%, which is high above the client’s hot utility saving demand, which is 30%. However, reaching this significant savings would presumably lead to significant modifications of current HEN and thus high investment cost. As the investment cost minimization is required, a utility saving lower than 52.3% is assumed.

#### 4.2. Retrofit Identification (RI Stage) of HEN–the Most Beneficial Utility Path Localization

_{max}evaluation of each Utility Path found in the RSGD. For this purpose, there was applied the Basic LP Model P1 for the Identification of Network Pinch published by Zhu and Asante [29]. This linear model allows finding R

_{max}(i.e., a suitable location for the new HE insertion) considering the specified EMAT value. Then, the results obtained by this model are sorted to the RIT in order from the most to the least beneficial (in terms of R

_{max}) Utility Path. RIT together with RSGD enables a very quick assessment of all feasible Utility Paths as well as the locations and heat duties of new heat exchangers creating the specific Utility Path. The basic results from RIT created for the studied oil hydrogenation process are summarized in Table 2.

#### 4.3. Detail Design (DD) Stage of the New Heat Exchanger (EN) Creating Most Beneficial Utility Path

## 5. Conclusions

## Author Contributions

## Funding

## Conflicts of Interest

## References

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Heat Exchanger | Unit | E1 | E2 | E3 | HU | CU_{tot} ^{1} |
---|---|---|---|---|---|---|

Geometry | ||||||

TEMA type | – | AES | AES | AES | ||

Number of shells in series-parallel | – | 1-1 | 1-2 | 1-1 | ||

Number of shell-tube passes | – | 1-4 | 1-4 | 1-4 | ||

Tube length | m | 5.5 | 6 | 6 | ||

Tube outer diameter/thickness | mm | 25/2.5 | 25/2.5 | 25/2.5 | ||

Tube layout angle | ° | 30 | 30 | 30 | ||

Tube pitch | mm | 32 | 32 | 32 | ||

Number of tubes | – | 80 | 80 | 80 | ||

Shell outside diameter | mm | 440 | 440 | 440 | ||

Baffle height | mm | 360 | 420 | 420 | ||

Baffle spacing | mm | 150 | 240 | 240 | ||

Number of baffles | – | 30 | 20 | 20 | ||

Process data | ||||||

Heat duty | kW | 239 | 1 226 | 236 | 1667 | 2344 ^{1} |

Heat transfer area | m^{2} | 34.5 | 75.4 | 37.7 | ||

Shell side stream | – | C1 | C2 | C3 | ||

Tube side stream | – | H2 | H1 | H3 | ||

Shell side heat transfer coeff. | W/m^{2}K | 303.2 | 497.4 | 198.7 | ||

Tube side heat transfer coeff. | W/m^{2}K | 382.7 | 1709.5 | 2531.1 | ||

Mean temperature difference | °C | 107 | 89.2 | 86.8 | ||

Overdesign ^{2} | % | 119.6 | 67.4 | 76.3 |

^{1}The value of CU

_{tot}(total cold utility) is given as a sum of the coolers CS1–3 heat duties.

^{2}To obtain the overdesign of the heat exchangers E1–3, the software HTRI was used.

Utility Path | R_{max} [kW] | HU [kW] ^{1} | HU Savings [%] | CU [kW] ^{1} | CU Savings [%] |
---|---|---|---|---|---|

H2-C2a | 2215.2 | 1152.8 | 30.8 | 1829.7 | 21.9 |

H3-C2a | 2039.9 | 1328.1 | 20.3 | 2004.9 | 14.5 |

H2-C2b | 1976.1 | 1391.8 | 16.5 | 2068.7 | 11.7 |

H3-C2b | 1906.4 | 1461.6 | 12.3 | 2138.5 | 8.8 |

H4-C2 | 1716.0 | 1716.0 | 0.9 | 2328.8 | 0.6 |

H2-C2c | Required value of EMAT is not achievable in this Utility Path | ||||

H3-C2c | Required value of EMAT is not achievable in this Utility Path |

^{1}HU and CU is the hot and cold utility total heat duty related to the specific Utility Path.

E1 [kW] | E2 [kW] | E3 [kW] | EN [kW] | R_{max} [kW] | HU Savings [%] | CU Savings [%] |
---|---|---|---|---|---|---|

239 | 1226 | 236 | 514.1 | 2215.2 | 30.8 | 21.9 |

**Table 4.**The heat duty results of exchanger EN obtained from the Retrofit Identification (RI) stage and Detail Design (DD) stage.

Retrofit Stage (Model) | Duty of EN [kW] | HU [kW] | HU Savings [%] |
---|---|---|---|

RI stage (LP model) | 514.1 | 1152.8 | 30.8 |

DD stage (nonlinear simulation) | 561.5 | 1105.4 | 33.7 |

Unit | EN Parameters Similar to E2 | Working Fluid Switch | Working Fluid Switch + Intensification | ||
---|---|---|---|---|---|

Heat duty | [kW] | 561.5 | 561.5 | 561.5 | |

Heat transfer area | [m^{2}] | 75.4 | 75.4 | 75.4 | |

Shell side heat trans. coeff. | [W/m^{2}K] | 241.28 | 119.33 | 292.9 | |

Tube side heat trans. coeff. | [W/m^{2}K] | 88.11 | 1395.5 | 1395.5 | |

Overdesign | [%] | −69.69 | −43.79 | +9.86 |

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**MDPI and ACS Style**

Jegla, Z.; Freisleben, V. Practical Energy Retrofit of Heat Exchanger Network Not Containing Utility Path. *Energies* **2020**, *13*, 2711.
https://doi.org/10.3390/en13112711

**AMA Style**

Jegla Z, Freisleben V. Practical Energy Retrofit of Heat Exchanger Network Not Containing Utility Path. *Energies*. 2020; 13(11):2711.
https://doi.org/10.3390/en13112711

**Chicago/Turabian Style**

Jegla, Zdeněk, and Vít Freisleben. 2020. "Practical Energy Retrofit of Heat Exchanger Network Not Containing Utility Path" *Energies* 13, no. 11: 2711.
https://doi.org/10.3390/en13112711