–(33))。 Also for the same reason, all the values related to cost are taken from the work of Caputo et al。 [6] who tried all the case studies by GA approach。
In the SA approach upper and lower bounds for the optimization variables are given in Table 1。 All the values of discounted operating costs are computed with ny = 10 yr, annual discount rate (i) = 10%, energy cost (Ce) = 0。12 €/kW h and an annual amount of work hours H = 7000 hr/yr。
Table 3 shows the optimized parameters of the case studies obtained using SA and comparison with the optimized parameters obtained by Caputo et al。 [6] using GA approach, while Figure 3 shows the cost comparison of both the approaches for all the three case studies。 From Table 3 it is clear that the pro- posed SA approach has ability to reduce the total cost
Table 2。 Process inputs and physical properties for different case studies
–3 –1 –1
–1 –1
2 –1
Condition Mass flow, kg/s Tinput / C Toutput / C / kg m Cp / kJ kg K / Pa s K / W m K Rfouling / m K W
Case 1
Shell side: methanol 27。80 95。00 40。00 750。00 2。84 0。00034 0。19 0。00033
Tube side: sea water 68。90 25。00 40。00 995。00 4。20 0。0008 0。59 0。0002
Case 2
Shell side: kerosene 5。52 199。00 93。30 850。00 2。47 0。0004 0。13 0。00061
Tube side: crude oil 18。80 37。80 76。70 995。00 2。05 0。00358 0。13 0。00061
Case 3
Shell side: oil 43。60 114。00 66。00 820。00 2。17 0。00024 0。13 0。00070
Tube side: cooling water 45。38 26。00 50。00 993。00 4。17 0。00068 0。63 0。00015
Table 3。 Optimal heat exchanger geometry using different optimization methods 模拟退火技术来设计英文文献和中文翻译(12):http://www.youerw.com/fanyi/lunwen_100221.html