模拟退火技术来设计英文文献和中文翻译(17)

30000 750S0。81 (52)

proach compared to GA approach considered by Ponce-Ortega et al。 [16]。

Various alternatives of exchangers

The solution space of cost objective function with multiple constraints is very much complicated with multiple local minima。 Cost wise these local mi- nima may be very near to each other but geometri- cally represent complete different sets of exchangers。 To assess these multiple local minima, the SA pro- gram was run 100 times with new starting guess every time。 For case study 2, i。e。, different sets of solutions vectors x is assumed in every run。 Most of the times SA converged to global minima but sometimes it were

found that it got stuck to local minima depending upon

Capital cost of pump ($) = (2000 5( t ΔP

t

)0。68 ) 

the complexity of solution space。 All these feasible solutions were collected and solution within 5% of mi-

(2000 5( s ΔP )0。68 ) (53)

nimum cost is presented in Table 4 for case study 2。

s From this table, it is clear that multiple heat exchanger configuration is possible with practically same cost or

Cost of power ($/W Hr):

Cpow 0。000045 (54) Pump efficiency:

70% (55)

Plant operation (h/year):

H = 8000 (56)

Annualization factor (/year):

Af 0。322 (57)

The design proposed by Ponce-Ortega et al。 [16] using GA approach assumed an exchanger with four tube side passages (with square pitch pattern) and one shell side passage。 The same configuration is not retained in the present approach and considers the tube side passes a free variable。 Results show increment of tube side and shell side heat transfer coefficient (5。26% on tube side and 88。7% on shell side) resulted in 23。85% increment in overall heat transfer coefficient in the present approach。 The higher overall heat transfer coefficient results in 19。52% re- duction in heat exchanger area and 20。83% reduction in heat exchanger length in the present approach compared to GA approach。 The capital investment is decreased by 3。69%。 Less pressure drop in tube side (due to shorter tube length) and less pressure drop in shell side (due to less number of baffles) resulted in 66。45% reduction in pumping cost as compared to GA approach。 In totality, the combined effect of capi- tal investment and operating costs results in 11。16% reduction in the total cost/year in the present ap-

with little cost difference。 All these solutions are feasible and the user has flexibility to choose any one of them based on his requirement and engineering judgment。 For example, some users have very less space available in his company, so they may choose the lowest length heat exchanger and fixed tube head, as they have no space available to use a pull through heat exchanger。 Selecting the best exchanger design from Table 4 is a combination of science and arts。 Decision of best exchanger selection for a parti- cular service and industry is based on multiple criteria including costs。 These criteria sometimes influence the best selection decision much more than the simple lowest cost criteria。 Maintainability, ease of cleaning of tubes and shells, less fouling tendency, flow in- duced vibrations, less floor space requirement, com- pactness of design, etc。, are some of these criteria which must be considered in an industrial scenario。 The lowest cost exchangers are not always perform- ing best in actual shop floor。 These criteria though very influential for final selection of exchanger are often qualitative and difficult to express quantitatively。 It requires designer experience, engineering judg- ment, customer requirements and normally very prob- lem specific。 Following section describes some of the criteria which can facilitate the user to select the best exchanger for his case studies。 These criteria are col- lected from literatures and based on experience of designers。 The final decision is dedicated to the user。模拟退火技术来设计英文文献和中文翻译(17):http://www.youerw.com/fanyi/lunwen_100221.html