A Novel Strategy for Simulating the Main Fractionator of Delayed Cokers by Separating the De-superheating Process

Yang, Lina; Zhang, Bingjian; Hou, Xiaoqiong; Chen, Qinglin

doi:10.1016/s1004-9541(13)60472-4

Cited by 6 publications

(4 citation statements)

References 15 publications

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“…For example, increasing the temperature of the LGO draw tray will raise the end point of the LGO and increase its yield while decreasing the HGO yield. As a result, changes in any of the variables in the fractionation section will have an influence on the other variables [21].…”

Section: Fractionation Sectionmentioning

confidence: 99%

Optimization of Delayed Coker Unit Process Variables for Enhancement of Product Yields

Mohamed,

Hassan

2024

Journal of Petroleum and Mining Engineering

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This study has been constructed using Aspen HYSYS ver.12.1 and regression analysis had been performed by MICROSOFT EXCEL 2010 to obtain a new correlations to predict the product yields from delayed coker unit with a wide applicable range of operating variables which is more reliable with refineries data and a simulation molding of delayed coker unit has been accomplished to maximize the gas oil yield for a refinery data by optimization of process variables. The findings from optimization by linear programming performed by MICROSFT OFFICE EXCEL 2010 indicated that gas oil yield could be increased by 4 wt% instead of coke byproduct by lowering the recycle ratio to 5% wt from fresh feed and increasing the heater outlet temperature to 510°C.Also the results showed that the change in coke drum pressure has a minimal effect in product yield. The outcome from the modified process conditions studied and a profit estimated at approximately 40 million dollar yearly.

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Section: Fractionation Sectionmentioning

confidence: 99%

Optimization of Delayed Coker Unit Process Variables for Enhancement of Product Yields

Mohamed,

Hassan

2024

Journal of Petroleum and Mining Engineering

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“…It is applicable for both vacuum tower and crude distillation tower. It is not suitable for Hydrogen systems but can be used for Hydrocarbon and light gas systems such as carbon dioxide and hydrogen sulfide [24]. The Grayson Stread Equation (GS) was the addition to the CHAO-SEA method to be applicable for hydrogen rich mixtures with high temperature and pressure systems up to 4700 K and 200 bar respectively [25].…”

Section: Thermodynamic Model Developmentmentioning

confidence: 99%

Thermodynamic Modeling and Process Simulation of Kumkol Crude Oil Refining

Jamali,

Bissenbay,

Nuraje

2023

Eurasian Chem.-Technol. J.

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The Crude Distillation Unit (CDU) mechanism is commonly regarded as the first stage in petroleum refining. In this study, Aspen Plus® is used to simulate the basic process of a CDU, which consists of an Atmospheric Distillation Column (ATC) and a Vacuum Distillation Column (VC). These columns are fed with two types of crude oil: KUMKOL from Kazakhstan and Soviet Export Blend, in the proportions of 0.75:0.25, 0.50:0.50, and 0.25:0.75, respectively. The goal was to do a parametric analysis and analyze the resultant streams of naphtha, kerosene, Atmospheric Gas Oil (AGO), Light Vacuum Gas Oil (LVGO), and Heavy Vacuum Gas Oil (HVGO). The simulation used the CHAO-SEA thermodynamic model, which included the Chao-Seader correlation, the Scatchard-Hildebrand model, the Redlich-Kwong equation of state, the Lee-Kesler equation of state, and the API gravity technique. Temperature, pressure, mass flow, enthalpy, vapor percentage, and average molecular weights of the streams at various phases within the CDU system were estimated. For both the ATC and VC columns, curves indicating Temperature- Pressure vs the number of stages, as well as ASTM D86 (temperature) versus stream volume % distillation, were developed. The results show that when compared to feed streams containing 0.25 and 0.50 StdVol of Kumkol Kazakhstan Oil, the feed stream with 0.75 StdVol produces more Heavy, Medium, and Light Vacuum Gas Oil (H-VGO, M-VGO, and L-VGO), as well as more Vacuum Gas (VG). These findings indicate that Kumkol Kazakhstan Oil is of high quality and has fewer contaminants, such as sulfur when compared to other accessible mixes throughout the world.

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“…The simulation system PRO/II has been used to model the steady state performance of the fractionator in the DCU . The operating conditions and some unknown parameters have been obtained from the simulation results of the fractionating process.…”

Section: Case Studymentioning

confidence: 99%

“…The simulation system PRO/II has been used to model the steady state performance of the fractionator in the DCU. 61 The operating conditions and some unknown parameters have been obtained from the simulation results of the fractionating process. From the flow sheet in Figure 6, the essential hot streams (to be cooled) and cold streams (to be heated) have been identified, and the stream data have been collected from the simulation results.…”

Section: Case Studymentioning

confidence: 99%

Simultaneous Optimization of the Complex Fractionator and Heat Exchanger Network Considering the Constraints of Variable Heat Removals in Delayed Coking Units

Yang

Zhang

et al. 2014

Ind. Eng. Chem. Res.

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Heat exchanger networks in process plants recover usable heat from hot to cold process streams such as feedstock, product, and pumparound streams. In this paper, we focus on the design of a heat exchanger network for removing variable heat from a complex fractionator in delayed coking units. A superstructure-based mixed integer nonlinear programming model is presented to minimize the total annual cost, including the heat exchanger area cost and the utility cost. In the proposed model, duties and operating parameters of pumparounds are optimized and the optimized structure of the heat exchanger network is defined simultaneously. Meanwhile, two modifications are applied to improve the simultaneous optimization model for the integrated system of the complex fractionator and heat exchanger network. First, a predominant calculation method for the log mean temperature difference is introduced in order to obtain the results closest to the actual process; second, nonconstant specific heat of process streams with pseudocomponents is considered to represent real thermal properties of process streams in the process model. A case study is carried out to demonstrate simultaneous optimization of the fractionator and heat exchanger network. The optimal design for the model is compared to the one with conventional design heuristics. By applying the proposed model to integrate the operation of the fractionator and heat exchanger network in a delayed coking unit, the total annual cost is reduced by 2.1 million CNY considering the constraints of the heat removals.

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A Novel Strategy for Simulating the Main Fractionator of Delayed Cokers by Separating the De-superheating Process

Cited by 6 publications

References 15 publications

Optimization of Delayed Coker Unit Process Variables for Enhancement of Product Yields

Optimization of Delayed Coker Unit Process Variables for Enhancement of Product Yields

Thermodynamic Modeling and Process Simulation of Kumkol Crude Oil Refining

Simultaneous Optimization of the Complex Fractionator and Heat Exchanger Network Considering the Constraints of Variable Heat Removals in Delayed Coking Units

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