#Capcost program software
)įigure A.2 Purchased Costs for Evaporators and Vaporizersįigure A.3 Purchased Costs for Fans, Pumps, and Power Recovery Equipment (Cost Data for Fans Takenfrom R-Books Software by Richardson Engineering services )įigure A.4 Purchased Costs for Fired Heaters and Furnacesįigure A.5 Purchased Costs for Heat Exchangersįigure A.6 Purchased Costs for Packing, Trays, and Demistersįigure A.7 Purchased Costs of Storage Tank and Process Vessels. Table A.1 Equipment Cost Data to Be Used with Equation A.1įigure A.1 Purchased Costs for Compressors and Drives (Cost Data for Compressors and Drives Takenfrom R-Books Software by Richardson Engineering Services, Inc. This form of the graph clearly illustrates the decreasingĬost per unit of capacity as the size of the equipment increases.
It should be noted that in these figures, the data areplotted as as a function of size attribute, A. These data are alsopresented in the form of graphs in Figures A.1A.17. The data for K1, K2, and K3, along with themaximum and minimum values used in the correlation, are given in Table A.1. Where A is the capacity or size parameter for the equipment. ĭata for the purchased cost of the equipment, at ambient operating pressure and using carbon steelconstruction,, were fitted to the following equation: The bare module factors for these units are taken tobe the field installation factors given by Guthrie. In general, these units are generally bought as apackage, and installation in the plant is not expensive. For this new equipment, bare module factors were not available, nor werepressure factors or materials of construction factors. The purchased costs for these types of equipment were obtained in 2003 but the costs given here havebeen normalized to 2001. Īll the data for the purchased cost of equipment for the second edition of this book were obtained from asurvey of equipment manufacturers during the period May to September of 2001, so an average value ofthe CEPCI of 397 over this period should be used when accounting for inflation.Īdditional process equipment has been added to the third edition and is listed below: Conveyors Crystallizers Dryers Dust Collectors Filters Mixers Reactors Screens The purpose of this appendix is to present the equations and figures that describe the relationships used inthe capital equipment-costing program CAPCOST introduced in Chapter 7 and used throughout the text.The program is based on the module factor approach to costing that was originally introduced by Guthrie and modified by Ulrich. Based on the current design, however, it is not recommended to move forward with this process.Appendix A Cost Equations and Curves for the CAPCOST Program Therefore, if this process is redesigned, it is recommended to design a process that requires less air flow or a lower pressure. The main utility cost originates from the cost of compressing the large amount of air flowing through the system. Although the maleic anhydride product is more profitable than the feed stream, the high annual utility cost of $39,100,000 causes a negative net present value for this process. It is recommended, based on the profitability analysis, that this process not be pursued further.
#Capcost program series
The desired solid maleic anhydride is purified using a series of cyclones. Maleic anhydride and several byproducts are produced from this reaction. This pure stream is mixed with oxygen in air and fed to the reactor. The process begins by feeding the mixed butane stream through two distillation columns to achieve pure n-butane. A catalyst, vanadium phosphorous oxide, assists in this reaction, adsorbing oxygen onto its surface to enable its reaction with n‑butane. Maleic anhydride is produced by the thermal oxidation of n-butane at an elevated temperature and pressure, in this case 375☌ and 20 bar.
#Capcost program plus
The simulation software Aspen Plus by AspenTech was the primary software used to design the plant, and the CAPCOST program in Microsoft suite’s Excel was utilized for the economic review of the process. This design team has been asked to produce a conceptual design, simulation, and profitability analysis for the proposed plant. The plant is to produce 40,000 metric tons per year of maleic anhydride from a mixture of excess butanes. Gamecock Chemical Company has proposed the construction of a maleic anhydride plant at its Houston refinery.