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Stanislav Boldyryev - One of the best experts on this subject based on the ideXlab platform.
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Cost Effective Heat Exchangers Network of Total Site Heat Integration
Chemical engineering transactions, 2016Co-Authors: Stanislav Boldyryev, Goran Krajačić, Neven DuićAbstract:This paper deals with selection of optimum amount Heat to be recovered during Total Site integration and utility targets for external Heating, cooling, refrigerating etc. The methodology provides the calculation of minimum capital investment during Heat integration of industrial site. It uses Heat Transfer Area targets, utility distribution with overall cost of retrofit. Heat Transfer Area is calculated for different regions with use of intermediate utility and direct Heating and cooling. Minimal temperature difference between Total Site profiles is analysed. Minimum of total Heat Transfer Area for Total Site recovery is calculated for array of minimal temperature differences. The utility consumption, numbers of units and material of equipment are analysed too and minimum total cost for retrofit project of site recovery system is calculated. The case study shows Heat recovery improvement on 1.94 MW. Site Heating demands is reduced on 37.3 % and cooling capacity reduction is 39.6 %. The implementation of retrofit EUR 777, 474 and payback time is 11.96 months.
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Cost Minimisation for Total Site Heat Recovery
Chemical engineering transactions, 2015Co-Authors: Stanislav Boldyryev, Goran Krajačić, Neven Duić, Petar Sabev VarbanovAbstract:In this paper minimisation of total cost for retrofit of Total Site Heat recovery system is proposed. It based on analysis of balanced Total Site Profiles and includes procedure for calculation of Heat Transfer Area. Heat Transfer Area is calculated for different regions with use of intermediate utility and direct Heating and cooling. Minimal temperature difference between Total Site Profiles is analysed. Global minimum of Heat Transfer Area for Total Site recovery is calculated for array of minimal temperature differences. It is analysed with utility consumption, numbers of units and material of equipment. Selection of minimum total cost for retrofit project of site recovery system is proposed.
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Targeting of Trade-Off for Total Site Heat Recovery
2015Co-Authors: Stanislav Boldyryev, Goran KrajačićAbstract:This paper deals with selection of optimum amount Heat to be recovered during Total Site integration and utility targets for external Heating, cooling, refrigerating etc. The methodology provides the calculation of minimum capital investment during Heat integration of industrial site. It uses Heat Transfer Area targets, utility distribution with overall cost of retrofit. Heat Transfer Area is calculated for different regions with use of intermediate utility and direct Heating and cooling. Minimal temperature difference between Total Site profiles is analysed. Minimum of total Heat Transfer Area for Total Site recovery is calculated for array of minimal temperature differences. The utility consumption, numbers of units and material of equipment are analysed too and minimum total cost for retrofit project of site recovery system is calculated. The case study shows Heat recovery improvement on 1.94 MW. Site Heating demands is reduced on 37.3% and cooling capacity reduction is 39.6%. The implementation of retrofit 777, 474 Euro and payback time is 11.96 months.
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Minimum Heat Transfer Area for Total Site Heat recovery
Energy Conversion and Management, 2014Co-Authors: Stanislav Boldyryev, Petar Sabev Varbanov, Andreja Nemet, Jiří Jaromír Klemeš, Petro KapustenkoAbstract:In this paper a further development of methodology for decreasing the capital cost for Total Site Heat recovery by use of different utility levels is proposed. The capital cost of Heat recovery system is estimated for certain temperature level of intermediate utility applying Total Site Profiles. Heat Transfer Area is reduced by selection of appropriate temperature of intermediate utility. Minimum of Heat Transfer Area depends on slopes of Total Site Profiles in each enthalpy interval. This approach allows estimating the minimum of Heat Transfer Area for Heat recovery on Total Site level. Case study is performed for fixed film Heat Transfer coefficients of process streams and intermediate utilities. It indicates that the total Heat Transfer Area of Heat recovery can be different up to 49.15% for different utility temperatures.
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Targeting Minimum Heat Transfer Area for Heat Recovery on Total Sites
Chemical engineering transactions, 2013Co-Authors: Stanislav Boldyryev, Petar Sabev Varbanov, Andreja Nemet, Petro Kapustenko, Jiří Jaromír KlemešAbstract:This paper upgrades the Total Site integration methodology, when accounting for a trade-off between capital and Heat recovery by selection of optimal temperature levels for intermediate utilities and therefore, decrease capital cost. Heat Transfer Area for recuperation in Total Site is a two-fold problem and it depends on the Sink Profile on one side and on the Source Profile on another. The resulting temperature of intermediate utility is a result of a trade-off since the Heat Transfer Area on Source side is decreasing, when temperature of IM is decreasing, however increased on Sink side. In the opposite higher intermediate utility temperature leads to higher Area on the Source side and lower on Sink side. The temperature of each intermediate utility may be varied between specified lower and upper bounds subject to serving the Sink and Source Profiles.
Petro Kapustenko - One of the best experts on this subject based on the ideXlab platform.
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Minimum Heat Transfer Area for Total Site Heat recovery
Energy Conversion and Management, 2014Co-Authors: Stanislav Boldyryev, Petar Sabev Varbanov, Andreja Nemet, Jiří Jaromír Klemeš, Petro KapustenkoAbstract:In this paper a further development of methodology for decreasing the capital cost for Total Site Heat recovery by use of different utility levels is proposed. The capital cost of Heat recovery system is estimated for certain temperature level of intermediate utility applying Total Site Profiles. Heat Transfer Area is reduced by selection of appropriate temperature of intermediate utility. Minimum of Heat Transfer Area depends on slopes of Total Site Profiles in each enthalpy interval. This approach allows estimating the minimum of Heat Transfer Area for Heat recovery on Total Site level. Case study is performed for fixed film Heat Transfer coefficients of process streams and intermediate utilities. It indicates that the total Heat Transfer Area of Heat recovery can be different up to 49.15% for different utility temperatures.
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Targeting Minimum Heat Transfer Area for Heat Recovery on Total Sites
Chemical engineering transactions, 2013Co-Authors: Stanislav Boldyryev, Petar Sabev Varbanov, Andreja Nemet, Petro Kapustenko, Jiří Jaromír KlemešAbstract:This paper upgrades the Total Site integration methodology, when accounting for a trade-off between capital and Heat recovery by selection of optimal temperature levels for intermediate utilities and therefore, decrease capital cost. Heat Transfer Area for recuperation in Total Site is a two-fold problem and it depends on the Sink Profile on one side and on the Source Profile on another. The resulting temperature of intermediate utility is a result of a trade-off since the Heat Transfer Area on Source side is decreasing, when temperature of IM is decreasing, however increased on Sink side. In the opposite higher intermediate utility temperature leads to higher Area on the Source side and lower on Sink side. The temperature of each intermediate utility may be varied between specified lower and upper bounds subject to serving the Sink and Source Profiles.
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Estimation of enhanced Heat Transfer Area targets in process industries
Computer Aided Chemical Engineering, 2013Co-Authors: Olga P. Arsenyeva, Petro Kapustenko, Robin Smith, Igor Bulatov, Leonid Tovazhnyanskyy, G. KhavinAbstract:Abstract Heat Transfer enhancement is one of the most promising methods to optimize Heat Transfer equipment and to increase Heat recovery in industrial processes. Plate Heat Exchanger (PHE) is one of established types of enhanced HEs. To estimate possible benefits of that kind of Heat Transfer enhancement, a mathematical model of PHE, which accounts for different plate types and corresponding corrugations geometry, is used. Based on this model the optimization algorithm was developed using MINLP method with inequality constraints. The objective function is the Heat Transfer Area of PHE unit. The plate spacing, plate length, the corrugations inclination angle to plate's vertical axis and the ratio of corrugations’ pitch to its height are the optimized variables. The developed algorithm is implemented as DLL module, which can be used for multiple calculations when optimizing Heat exchanger networks (HEN).
Sergio Mussati - One of the best experts on this subject based on the ideXlab platform.
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nlp modeling for the optimization of libr h2o absorption refrigeration systems with exergy loss rate Heat Transfer Area and cost as single objective functions
Energy Conversion and Management, 2016Co-Authors: Sergio Mussati, Krist V. Gernaey, Miguel C MussatiAbstract:Abstract Based on a nonlinear mathematical programming model, the sizes and operating conditions of the process units of single-effect absorption refrigeration systems operating with a LiBr–H 2 O solution are optimized for a specified cooling capacity by minimizing three single objective functions: the total exergy loss rate, the total Heat Transfer Area, and the total annual cost of the system. It was found that the optimal solution obtained by minimization of the total exergy loss rate provides “theoretical” upper bounds not only for the total Heat Transfer Area of the system but also for each process unit and all stream temperatures, while the optimal solution obtained by minimization of the total Heat Transfer Area provides the lower bounds for these model variables, to solve a cost optimization problem. The minimization of the total exergy loss rate by varying parametrically the available total Heat Transfer Area between these bounds was also performed, allowing to see how the optimal distribution of the available total Heat Transfer Area among the system components, as well as the operating conditions (stream temperature, pressure, composition, and mass flow rate) and Heat loads, vary qualitatively and quantitatively with increasing available total Heat Transfer Area. These optimization results allowed to find a “practical” value of the total Heat Transfer Area, i.e. no benefits can be obtained by increasing the available total Heat Transfer Area above this value since the minimal total exergy loss value cannot be significantly improved by distributing additional Heat Transfer Area among the process units. The optimal solution corresponding to this practical value significantly improves the upper bounds for an economic optimization problem with respect to the optimal solution corresponding to the theoretical value. The optimal solutions corresponding to the theoretical and the practical upper bound values for the total Heat Transfer Area (100 m 2 and 61 m 2 , respectively) as well as the optimal solution obtained by minimization of the total annual cost are discussed for a case study considering a cooling capacity of 50 kW, upon the model assumptions made and a given cost model. Around three-quarters of the minimal total annual cost correspond to capital expenditures and the rest to operating expenditures. The generator and evaporator represent together around 70% of the capital expenditures. The absorber is the largest contributor to both the total Heat Transfer Area and the total exergy loss rate, with around 33.19 and 39.16%, respectively, when the total annual cost is minimized.
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a discrete and continuous mathematical model for the optimal synthesis and design of dual pressure Heat recovery steam generators coupled to two steam turbines
Energy, 2016Co-Authors: Juan I. Manassaldi, Miguel C Mussati, Nicolás J. Scenna, Ana M Arias, Sergio MussatiAbstract:This paper addresses the optimal arrangement and design of a dual pressure Heat recovery steam generator coupled to two steam turbines. A superstructure that embeds various alternative configurations is optimized considering the following two single objective functions: (a) the maximization of the total net power generation for a given total Heat Transfer Area and (b) the minimization of the total Heat Transfer Area for a given total net power. The optimal number of Heat exchangers and pumps and how they should be connected are the discrete decisions. The dimensions and operating conditions are the continuous decisions. A discrete and continuous mathematical model is developed and logical propositions are used for discrete decisions. The results are compared with a reference case reported by other authors. The results indicated that the optimization of the proposed superstructure allowed to find a more efficient HRSG configuration. The obtained configurations differ from the configuration of the reference case in how the Heat exchangers and pumps are connected. A considerable increase in about 8% of the total net power generation in (a) and a significant reduction in about 24% of the total Heat Transfer Area in (b) are achieved when compared to the reference case.
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Optimization mathematical model for the detailed design of air cooled Heat exchangers
Energy, 2014Co-Authors: Juan I. Manassaldi, Nicolás J. Scenna, Sergio MussatiAbstract:This paper presents a disjunctive mathematical model for the optimal design of air cooled Heat exchangers. The model involves seven discrete decisions which are related to the selection of the type of the finned tube, number of tube rows, number of tube per row, number of passes, fins per unit length, mean fin thickness and the type of the flow regime. Each discrete decision is modeled using disjunctions, boolean variables and logical propositions. The main continuous decisions are: fan diameter, bundle width, tube length, pressure drops and velocities in both sides of the ACHE, Heat Transfer Area, fan power consumption. Then, the resulting generalized disjunctive programming model is reformulated as a mixed integer non-linear programming, implemented in GAMS (general algebraic modeling system) and solved using a branch-and-bound method. The proposed model was successfully verified by comparing the obtained output results with different designs taken from the literature. Then, the model is solved to obtain the optimal designs corresponding to the following optimization criteria: a) minimization the total annual cost which includes investment (Heat Transfer Area) and operating cost (fan power consumption), b) minimization the Heat Transfer Area and c) minimization the fan power consumption. Obtained optimal and sub-optimal designs are compared in detail.
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NLP model-based optimal design of LiBr–H2O absorption refrigeration systems
International Journal of Refrigeration, 2014Co-Authors: María S. Mazzei, Miguel C Mussati, Sergio MussatiAbstract:Abstract This paper addresses the optimization of a single effect absorption refrigeration system operating with lithium bromide-water solution. A non-linear programming mathematical model is developed to determine the operating conditions and the distribution of the total Heat Transfer Area (sizes) along the involved process units to optimize the following two objective functions: (i) maximization of the coefficient of performance for a given amount of the total Heat Transfer Area, and (ii) minimization of the total Heat Transfer Area of the system for a given cooling capacity. The proposed model can either be used for simulation or optimization purposes. Simulated or optimized values of temperature, pressure, composition and flow rate of all streams and sizing of each process unit are predicted. In addition, because of the non linear nature of the resulting model, a systematic solution procedure is proposed in order to guarantee the model convergence. A detailed discussion of the optimization results are presented through different case studies.
Lin Cheng - One of the best experts on this subject based on the ideXlab platform.
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optimization design of Heat recovery systems on rotary kilns using genetic algorithms
Applied Energy, 2017Co-Authors: Qian Yin, Lin ChengAbstract:Heat loss from rotary kilns accounts for certain amounts of the total energy consumption in chemical and metallurgical industries. To reduce the Heat loss, a parallel and a series-parallel Heat recovery systems with nine Heat recovery exchangers are proposed to preHeat the cold water in this paper. Experimental measurements are carried out to determine the Heat Transfer coefficient equations of each Heat recovery exchanger. Then, the Heat recovery systems are analyzed to deduce the mathematic relation between the design parameters and the system requirements, i.e. the temperatures and Heat Transfer rates of the nine Heat recovery exchangers. The total Heat Transfer Area, the total power consumption and the entropy generation due to Heat Transfer and fluid flow are set as the objective functions in four multi-objective optimization (MOO) cases. With the aid of the genetic algorithm in the Matlab 2015, the optimized operational and structural parameters are obtained. Finally, the MOO results are compared with that of the single objective optimization (SOO) method and the original values. The optimization results show that the MOO method are more suitable for the operational parameters design of the Heat recovery systems compared with the SOO method. The required total Heat Transfer Area and the total power consumption are decreased by at least 12.1% and 13.7%, respectively. Besides, as the entropy generation due to Heat Transfer and fluid flow decrease in the MOO cases, the corresponding Heat Transfer Area and power consumption of the Heat recovery system decrease, respectively.
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design requirements and performance optimization of waste Heat recovery systems for rotary kilns
International Journal of Heat and Mass Transfer, 2016Co-Authors: Qian Yin, Qun Chen, Lin ChengAbstract:Abstract Heat loss from the shell of a rotary kiln accounts for a certain proportion of total energy consumption. In order to reduce Heat loss, a practical Heat recovery system with nine Heat exchangers is proposed to preHeat water in this paper. We first propose a mathematic model to analyze the shell temperatures and Heat loss rates of several regions on rotary kilns. Integration of theoretical analyses and experimental measurements yields the temperatures and Heat Transfer rates of Heat exchangers, i.e. the design requirements of the nine Heat exchangers in the practical system. Secondly, an optimization model is formed to describe the relation between design parameters, i.e. Heat Transfer Area and mass flow rate of each Heat exchanger, and system requirements without introducing any intermediate temperatures. With the aid of the Lagrange multiplier method, the optimal design parameters are obtained. Finally, an optimization case of the practical system is studied. The results show that the Heat recovery system should meet the requirements of chemical reactions in rotary kilns and mechanical characteristic of shell. The required total Heat Transfer Area of the system after optimization is reduced by 15.6% compared to the value before optimization. As the total mass flow rate increase and inlet temperature decreases, the required Heat Transfer Area decreases while the mass flow distribution ratios remains unchanged.
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The entransy dissipation minimization principle under given Heat duty and Heat Transfer Area conditions
Chinese Science Bulletin, 2010Co-Authors: Jiangfeng Guo, Lin ChengAbstract:Under given Heat duty and Heat Transfer Area conditions, the equipartition of the entransy dissipation (EoED) principle, the equipartition of the temperature difference (EoTD) principle, and the equipartition of the Heat flux (EoHF) principle are applied to the optimization design of a Heat exchanger with a variable Heat Transfer coefficient. The results show that the difference between the results obtained using the EoED and EoTD principles is very small, far smaller than that between the results obtained using the EoED and EoHF principles. The correct entransy dissipation minimization principle is chosen to optimize the parameters in the hot and cold fluids in a two-fluid Heat exchanger, under given Heat duty and Heat Transfer Area conditions. The results indicate that the proper choice of the two alternative fluids has an important role in the successful application of the entransy dissipation minimization principle. The fluid that could improve the total Heat Transfer coefficient should be chosen, or the fluid that makes the temperature profiles of the hot and cold fluids parallel and decreases the temperature difference between the hot and cold fluids after optimization simultaneously, could be the proper one.
Petar Sabev Varbanov - One of the best experts on this subject based on the ideXlab platform.
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Cost Minimisation for Total Site Heat Recovery
Chemical engineering transactions, 2015Co-Authors: Stanislav Boldyryev, Goran Krajačić, Neven Duić, Petar Sabev VarbanovAbstract:In this paper minimisation of total cost for retrofit of Total Site Heat recovery system is proposed. It based on analysis of balanced Total Site Profiles and includes procedure for calculation of Heat Transfer Area. Heat Transfer Area is calculated for different regions with use of intermediate utility and direct Heating and cooling. Minimal temperature difference between Total Site Profiles is analysed. Global minimum of Heat Transfer Area for Total Site recovery is calculated for array of minimal temperature differences. It is analysed with utility consumption, numbers of units and material of equipment. Selection of minimum total cost for retrofit project of site recovery system is proposed.
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Minimum Heat Transfer Area for Total Site Heat recovery
Energy Conversion and Management, 2014Co-Authors: Stanislav Boldyryev, Petar Sabev Varbanov, Andreja Nemet, Jiří Jaromír Klemeš, Petro KapustenkoAbstract:In this paper a further development of methodology for decreasing the capital cost for Total Site Heat recovery by use of different utility levels is proposed. The capital cost of Heat recovery system is estimated for certain temperature level of intermediate utility applying Total Site Profiles. Heat Transfer Area is reduced by selection of appropriate temperature of intermediate utility. Minimum of Heat Transfer Area depends on slopes of Total Site Profiles in each enthalpy interval. This approach allows estimating the minimum of Heat Transfer Area for Heat recovery on Total Site level. Case study is performed for fixed film Heat Transfer coefficients of process streams and intermediate utilities. It indicates that the total Heat Transfer Area of Heat recovery can be different up to 49.15% for different utility temperatures.
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Targeting Minimum Heat Transfer Area for Heat Recovery on Total Sites
Chemical engineering transactions, 2013Co-Authors: Stanislav Boldyryev, Petar Sabev Varbanov, Andreja Nemet, Petro Kapustenko, Jiří Jaromír KlemešAbstract:This paper upgrades the Total Site integration methodology, when accounting for a trade-off between capital and Heat recovery by selection of optimal temperature levels for intermediate utilities and therefore, decrease capital cost. Heat Transfer Area for recuperation in Total Site is a two-fold problem and it depends on the Sink Profile on one side and on the Source Profile on another. The resulting temperature of intermediate utility is a result of a trade-off since the Heat Transfer Area on Source side is decreasing, when temperature of IM is decreasing, however increased on Sink side. In the opposite higher intermediate utility temperature leads to higher Area on the Source side and lower on Sink side. The temperature of each intermediate utility may be varied between specified lower and upper bounds subject to serving the Sink and Source Profiles.