Heat exchangers - basics for efficient heat integration Introduction to modeling of heat exchangers SimulateLive. Energy efficiency in heat exchanger design Due to increased need for energy efficiency over the last years, more attention has been put tp the optimization of heat exchanger network. Heat exchangers in numerous engineering applications are just one of many components of a system.
The process energy requirement and cost are calculated from the mass balances, energy balances and the economic model of flowsheet. The flowsheet under investigation includes steam generation unit, gasification unit and gas cleaning unit.
For heat integration studies on the flowsheet, the pinch analysis is employed to obtain the energy efficient and self- sustained system. The analysis shows that considerable saving can be obtained for steam production using heat integration application as there is a large amount of available waste heat from the gas cleaning and cooling units.
The results show that the minimum hot utilities required is Furthermore, a feasible heat exchanger network that fulfills these requirements has been presented. Moreover, the cost of hydrogen production decreases from 1. Biomass steam gasification for hydrogen production is not only in favor of more hydrogen but also economical than other conventional gasifying methods and pyrolysis Balat, Furthermore, hydrogen purity can be increased in the product gas with in situ C02 capture technique using CaO as sorbent Florin and Harris, The hydrogen production cost can be reduced with energy efficient system through increasing thermal integration of the system Eljack et al.
The model incorporated the flowsheet mass, energy balances and heat and power integration. The thermo economic analysis showed that high efficiency process could be attained using heat integrated configurations.
They used pinch analysis method for the calculation of optimal internal heat recovery within the Please cite this article as: Fu and Gundersen, applied heat integration using pinch analysis on heat exchangers in an oxy-combustion process of coal fired power plant.
The technology provided high efficiency and low operating cost. The objective of the present work is to apply process integration in the flowsheet design for enriched hydrogen production from EFB via steam gasification with C02 capture in a single pass fluidized bed gasifier.
The feasibility of the process is investigated via parametric studies of energy recovery on the hydrogen cost using MATLAB. Pinch analysis approach is employed to integrate heat sources and sinks, to determine energy targets and to identify potential improvement in the flowsheet to obtain lower production cost and increased energy efficiency and self-sustainability.
Process Development The process flowsheet diagram was presented by authors in earlier work Inayat et al. EFB is used as the feedstock biomass and is pretreated i.
The gasifier operates at atmospheric pressure and assumed to be at steady state condition Inayat et al. Steam is used as the gasification agent, produced in a steam generator and superheated using super heaters.
The product gas from the gasifier is cooled down by passing it through a scrubber, and hydrogen recovered and purified using a pressure swing adsorption PSA unit. The steam gasification process is an endothermic process which requires external energy that is supplied using heaters.
Cost Minimization The minimum hydrogen production cost is solved subject to the process constraints Inayat et al. The minimum production cost of 1. The hydrogen yield and purity at the optimal condition are 0.
For heat integration studies on the flowsheet, the pinch analysis is employed to obtain the required minimum utilities. The stream data are extracted from the energy balance of the flowsheet at the optimum conditions with minimum hydrogen production cost calculated in the previous section.
The energy balance on the flowsheet is shown in Figure 1. Sankey diagram of energy balance for the flowsheet. The table shows that energy required for cold streams CI and C2 are and kJ respectively.
CI is the stream for super heated steam generation and C2 is the energy required to the gasification process. HI is the hot stream from scrubber. Stream data Stream Name Supply Temp. The calculation is performed with the minimum temperature difference of 10 K.
It can be calculated based on the composite curves that the minimum hot utilities required is There are three heat exchangers required to fulfil minimum amount of hot and cold utilities with the temperature difference of 10 K.
Optimized heat exchanger network Based on the matching in the developed HEN, the heat integrated process flowsheet design as shown in Figure 4 is proposed. The production cost of hydrogen is recalculated for the heat integrated flowsheet.
It is observed that by using heat integration, the hydrogen cost decreases from 1. So, using heat integration application, the flowsheet not only becomes energy efficient and self- sustained but also offers lower hydrogen production cost.Solar Heat Integration in Industrial Processes is a collaborative project of the IEA’s Solar Heating and Cooling, Task 49, and SolarPACES Program.
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Parallel to this graphical approach, mathematical optimization methods were developed to handle the same heat integration problems.
Initially, they. After heat integration has been optimized, further reduction of energy consumption can be achieved in the third shell: the heat pump (HP). A heat pump is a device that upgrades heat from a lower.