Costs of Individual Equipment

Couper, James R.; Penney, W. Roy; Fair, James R.; Walas, Stanley M.

doi:10.1016/b978-0-12-396959-0.00021-5

Cited by 30 publications

(11 citation statements)

References 1 publication

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“…The bare module cost of the NH 3 synthesis loop in the RXN-ABS process is calculated according to the method of Couper et al, 42 and the detailed dimensions, materials, quantities, and estimation formulas of the equipment are listed in Tables S7 and S10. Figure 7 shows the bare module cost in the RXN-CON, RXN-ADS, and RXN-ABS processes.…”

Section: ■ Results and Discussionmentioning

confidence: 99%

Techno-Economic Evaluation of Green NH₃ Production by Integrating Current-Assisted Reaction and Ionic Liquid Absorption

Song,

Zeng,

et al. 2024

ACS Sustainable Chem. Eng.

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In this work, an ammonia (NH 3 ) synthesis loop under mild conditions (595 K and 20 bar) was constructed, including a current-assisted reaction unit and a separation unit based on ionic liquid absorption. ASPEN Plus was used to simulate the NH 3 synthesis loop with a capacity of 20,000 tons per year, where the reactor was a customized model. Based on the simulation results, the techno-economic evaluation of a miniaturized green NH 3 production plant was carried out, with hydrogen from water electrolysis and nitrogen from pressure swing adsorption. The levelized cost of ammonia (LCOA) in the reaction-absorption (RXN-ABS) process was obtained to be 838.81 $ t NH3 −1 . The LCOA in the RXN-ABS process is 18.56% and 10.09% lower than the reported reaction-condensation (RXN-CON) and reaction-adsorption (RXN-ADS) processes, respectively. If the revenue from oxygen sales is taken into account, the RXN-ABS process can achieve an after-tax return of 34.72%. As the price of renewable electricity decreases to 0.024 $ kWh −1 and electricity consumption of water electrolysis decreases to 5.58 kWh kg NH3 −1 , the LCOA in the RXN-ABS process can be lower than the selling price of NH 3 . The new NH 3 synthesis loop has better economy and safety, which promotes the popularization of the distributed NH 3 production technology.

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Section: ■ Results and Discussionmentioning

confidence: 99%

Techno-Economic Evaluation of Green NH₃ Production by Integrating Current-Assisted Reaction and Ionic Liquid Absorption

Song,

Zeng,

et al. 2024

ACS Sustainable Chem. Eng.

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“…The direct and indirect costs of all equipment are according to Couper et al 32 and Sieder et al, 33 and materials of construction for the units are decided based on Biegler et al 34 The cost of the acid scrubber and dust control unit is obtained from a local vendor in India (www.indiamart.com website). 35 The cost of the alkaline scrubber is adapted from the literature.…”

Section: Process Modeling and Flowsheet Simulationmentioning

confidence: 99%

Techno-Economic and Life Cycle Assessment of Pyrolysis of Unsegregated Urban Municipal Solid Waste in India

Chhabra

Parashar

Shastri

et al. 2021

Ind. Eng. Chem. Res.

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This work performs detailed techno-economic and life cycle assessment (LCA) of pyrolysis of unsegregated (mixed) municipal solid waste (MSW) in the Indian context. Experimental results of thermal pyrolysis of a representative MSW sample generating char, oil, and gas are used. The proposed process uses gas internally for heating while oil and char are the products. The detailed process flowsheet for a 200 tonnes per day MSW pyrolysis processing plant is developed considering various heat integration and design considerations, and the process is simulated using ASPEN Plus. Experimental results are used to simulate the pyrolysis reactor. The plant is found to be energy sustainable for the moisture content in MSW less than 20% (w/w). The experimental and simulation data are then used to perform economic and LCA. The economic analysis suggests that the process is economically viable with a payback period of 6.17 years and an internal rate of return of 14.33%. However, the economics of the plant is highly sensitive to fluctuation in the installation cost of the reactor, oil collection efficiency, and the selling price of pyrolysis oil. The life cycle climate change impact is 250.4 kg CO 2 equiv/tonne of the MSW processed. As compared to open dumping and sanitary landfilling, pyrolysis shows an avoided impact of 989.6 and 593.6 kg CO 2 equiv/tonne of MSW, respectively. Based on these results, which are specific to the case study presented, it can be argued that pyrolysis of mixed MSW has potential for scale-up, and must be evaluated for other regions as well.

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“…The annualized area cost is given by the following linear equation, which is adopted from Couper et al where PB year is the payback period, and MF is the multiplication factor accounting for installation costs, construction, contingencies, and so forth.…”

Section: Model Descriptionmentioning

confidence: 99%

Simultaneous Optimization for Organic Rankine Cycle Design and Heat Integration

Dong

Liao

Sun

et al. 2020

Ind. Eng. Chem. Res.

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Organic rankine cycle (ORC) has been regarded as the most promising measure for converting low-grade waste heat into electricity during the past decades. To take better advantage of ORC, the parameters of ORC and its heat integration with the background process streams should be optimized simultaneously. In this work, the decision variables of ORC not only include the operating temperature, pressure, and flowrate but also contain the type of working fluids. A set of 43 pure fluids and 36 binary mixtures are adopted from the literature as candidates for working fluids. In addition, both the supercritical and subcritical conditions of ORCs are involved. Background process streams and ORC streams with variable temperatures and flowrates are synthesized for heat integration. Such a complicated heat integration problem cannot be solved by traditional methods, where the temperature and flowrates of streams are fixed. We develop a two-level optimization strategy. The outer level identifies the promising working fluids and their compositions, temperatures, and pressures inside the ORC. The inner level deals with the heat integration problem, where the temperatures and flowrates of streams are the variables. The flowrate of ORC, the utility consumption, as well as area of heat exchangers are optimized in the inner level based on the vertical heat transfer assumption of pinch technology. The outer level is solved by a genetic algorithm, while the inner level is solved by a deterministic algorithm. Case studies show that the inner level model for heat integration is superior in both efficiency and quality of the solution. We also provide an overview of the best ORC selection for a single waste heat source between 100 and 300 °C and show applicability for the integration of ORC and background processes with multiple streams in case studies.

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Costs of Individual Equipment

Cited by 30 publications

References 1 publication

Techno-Economic Evaluation of Green NH₃ Production by Integrating Current-Assisted Reaction and Ionic Liquid Absorption

Techno-Economic Evaluation of Green NH₃ Production by Integrating Current-Assisted Reaction and Ionic Liquid Absorption

Techno-Economic and Life Cycle Assessment of Pyrolysis of Unsegregated Urban Municipal Solid Waste in India

Simultaneous Optimization for Organic Rankine Cycle Design and Heat Integration

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Costs of Individual Equipment

Cited by 30 publications

References 1 publication

Techno-Economic Evaluation of Green NH3 Production by Integrating Current-Assisted Reaction and Ionic Liquid Absorption

Techno-Economic Evaluation of Green NH3 Production by Integrating Current-Assisted Reaction and Ionic Liquid Absorption

Techno-Economic and Life Cycle Assessment of Pyrolysis of Unsegregated Urban Municipal Solid Waste in India

Simultaneous Optimization for Organic Rankine Cycle Design and Heat Integration

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Product

Resources

About

Techno-Economic Evaluation of Green NH₃ Production by Integrating Current-Assisted Reaction and Ionic Liquid Absorption

Techno-Economic Evaluation of Green NH₃ Production by Integrating Current-Assisted Reaction and Ionic Liquid Absorption