浙江化工
浙江化工
절강화공
ZHEJIANG CHEMICAL INDUSTRY
2012年
4期
15-19,9
,共6页
管道化溶出%预热级数%年总费用%优化计算%新蒸汽用量
管道化溶齣%預熱級數%年總費用%優化計算%新蒸汽用量
관도화용출%예열급수%년총비용%우화계산%신증기용량
tube digestion%preheating stage%total annual cost%optimum mathematical model%live steam consumption
通过对拜耳法氧化铝生产的管道化溶出过程热平衡的模拟计算,分析了不同预热级数对新蒸汽用量、换热面积及总设备费用的影响。建立了以年总费用（包括年设备折旧费、维修费、蒸汽费用及电费等）最小为优化目标、预热与闪蒸级数（n）为决策变量的优化计算模型。某典型条件下的计算结果表明,n从5增加至16,新蒸汽用量减少了20.4%,总换热面积增加近29.0%,年总费用先减小后增大,过程最经济级数为11。敏感性分析显示,新蒸汽的单价对优化结果影响显著,其变化±50%会引起年总费用变化±22%以上,同时最经济级数由8变至14。
通過對拜耳法氧化鋁生產的管道化溶齣過程熱平衡的模擬計算,分析瞭不同預熱級數對新蒸汽用量、換熱麵積及總設備費用的影響。建立瞭以年總費用（包括年設備摺舊費、維脩費、蒸汽費用及電費等）最小為優化目標、預熱與閃蒸級數（n）為決策變量的優化計算模型。某典型條件下的計算結果錶明,n從5增加至16,新蒸汽用量減少瞭20.4%,總換熱麵積增加近29.0%,年總費用先減小後增大,過程最經濟級數為11。敏感性分析顯示,新蒸汽的單價對優化結果影響顯著,其變化±50%會引起年總費用變化±22%以上,同時最經濟級數由8變至14。
통과대배이법양화려생산적관도화용출과정열평형적모의계산,분석료불동예열급수대신증기용량、환열면적급총설비비용적영향。건립료이년총비용（포괄년설비절구비、유수비、증기비용급전비등）최소위우화목표、예열여섬증급수（n）위결책변량적우화계산모형。모전형조건하적계산결과표명,n종5증가지16,신증기용량감소료20.4%,총환열면적증가근29.0%,년총비용선감소후증대,과정최경제급수위11。민감성분석현시,신증기적단개대우화결과영향현저,기변화±50%회인기년총비용변화±22%이상,동시최경제급수유8변지14。
The effect of preheating stage on live steam consumption,heat transfer area and equipment costs was studied by computation of heat balance of Bayer tube digestion system.The optimum mathematical model of tube-heating retention-tank digestion was established,which aimed at the minimization of the total annual cost（TAC,including the costs of live steam,power,equipment depreciation and maintenance） and based on the preheating stage（n） as decision variable.The practical example indicated that when n increased from 5 to 16,the live steam consumptions decreased by 20.4%,however,the total heat transfer areas increased by about 29.0%,while n=12,the TAC is minimum,which might be considered as the economical preheating stage（nopt） under the given conditions.Through sensitivity analysis,it was found that the live steam price significantly affected the result,which changed ±50% would cause the changes in TAC over ±50% and made nopt shift from 8 to 14.
