增加炼油厂能效

1、增加炼油厂能效Slide 2Outline of presentation讲演议题Energy consumption in refining process 炼油厂能耗分布Process heat exchangers why change from shell and tube to Compabloc? 为什么管壳式工艺换热器可以被Compabloc替代？Energy savings possibility in refinery 炼油厂节能的可行性Individual exchangers换热器点对点的替换Process integration 换热网络优化Success storie

2、s in China 中国安装案例分析Summary 总结Slide 3Energy consumption in refining,炼油厂能耗分布source EIA, USAProcessAverage UsebCapacityAnnual EnergyConsumption% (103 Btu/bbl)(106 bbl/day)c(1012 Btu/year)AtmosphericDistillationd113.815.45641.626%Vacuum Distillation91.57.15238.810%Visbreakinge1990.06512.070%Delayed Coki

3、ng1661.671114.65%Fluid Coking 2580.0757.10%Flexicoking 1670.1126.70%FCC1005.2190.68%Hydrocracking2401.3109.74%Hydrotreating12010.7468.319%Reforming2843.6376.315%Alkylation7361.1148.86%Ethers Production4030.1833.41%Isomerization10100.518402%Lube Oil 15060.2109.54%TOTALf-2487.5100%Slide 4Why change fr

4、om shell and tube to Compabloc heat exchanger?为什么管壳式工艺换热器可以被Compabloc替代？Slide 5Possible to replace multiple shell and tube in series by one Compabloc unit一台Compabloc替代多台管壳式换热器成为可能Energy savings possibility in refinery 炼油厂节能的可行性Compabloc design and customer value Compabloc换热器设计理念和客户获得的价值 OutInOutInT1

5、T2T1T2Close temperature approach: down to 5C 温度端差可以达到5C Temperature cross 温度交叉 (T in - T out ) MTDNTU =MTDSlide 6PetroPlus, UKAtmospheric distillation unit 常减压装置Atmospheric residue常渣 300 000 kg/h 16590 C, PD 80 kPaBoiler feed water锅炉给水 140 000 kg/h 14850 C, PD 60 kPa2 Compabloc in SS 316L/320 m2两台31

6、6L材质，单台换热面积320m2In continuous operationsince beginning of 2002.2002年开始投用Slide 7液液热量回收案例 PetroPlus, UKqConventional case design with S&T 管壳式设计Residue 常渣 165 103 C NTU = 1.6BFW 锅炉给水 132 60 CNTU = 1.9Recovered heat 回收热量= 12 MWqIncreased case design with Compabloc Compabloc设计设计 Residue 常渣 165 90 C N

7、TU = 3.3BFW锅炉给水 148 60 C NTU = 3.8Recovered heat 回收热量= 14.5 MWqIncreased heat recovery of 2.5 MW 多回收热量2.5MWq2 Compablocs in parallel alt. 4 S&T in series. 两台Compabloc替代两串两并共四台管壳式换热器Slide 8Water120 C179 C180 C215 CSteamSuperheated steamMid-pump-around (MPA)221 CMPA220 CMPA 186 CMPA181 CExxonMobil

8、, Netherlands - Hydrocracker 加氢裂化装置Compabloc for Steam generation 蒸汽发生器 MPA 221 220 CSteam 215 180 CMPA 220 186 CSteam gen. 180 179 CMPA 186 181 CWater 179 120 CWater heatingSteam generationSteam super-heating15 tons/hour of 9 bar steam produced. Totally 8.4 MW recovered. 发生的蒸汽相当于回收热量8.4MWSlide 9Sli

9、de 10ExxonMobil, Netherlands - Hydrocracker Compabloc for Steam generation 蒸汽发生器Steam generator蒸汽发生器Water pre-heater 水预热器Start Up: 2002 开车时间2002年Slide 11New Building Atmospheric distillation新建的常减压蒸馏装置Petroleum Gas & Light NaphthaHeavy NaphthaKeroseneLight Gas Oil (LGO)Heavy Gas Oil (HGO)Atmosphe

10、ric residuePreheated Crude oilDistillation towerFired heaterCrude oil feed120C25-175C150-260C235-360C330-380C280-300C350-370CSlide 12Layout of crude preheat trainsource NPRA paper, USA, 200625oC120oC120oC210oC195-200oC280-300oCSlide 13China Case Studies in ADU/VDU Plant中国常减压装置案例分析Slide 14空冷空冷常常压压塔塔塔

11、顶油罐125 C60 C91 C40 C70C90 C32 C40 C循环水循环水塔顶油气塔顶油气Case study for top condenser 塔顶油气换热器塔顶油气换热器 案例分析案例分析热水热水塔顶三注塔顶三注115 CSlide 15空冷空冷常常压压塔塔塔顶油罐125 C60 C84 C40 C70C95 C32 C43 CCase study for top condenser 塔顶油气换热器塔顶油气换热器 案例分析案例分析120 C循环水循环水塔顶油气塔顶油气热水热水塔顶三注塔顶三注Slide 16热水出口温度，C油气冷后温度，C 循环水出口温度，C90914095844

12、3换热器台数换热器材质净重/安装质量，吨换热器一次投资（不包括节约的管线、阀门、设备基础、安装空间）1009钢298/3501004SMO254/316L46/5280%Slide 17Slide 18初馏塔说明：该加热流程需要管壳式换热器说明：该加热流程需要管壳式换热器26台。其中台。其中304材质为材质为4台，台，316L材质为材质为18台，台，317L为为4台。价格为台。价格为5400万人民币。不锈钢阀门为万人民币。不锈钢阀门为104个（不含跨线阀门），价格未计算在内个（不含跨线阀门），价格未计算在内初底油 196295CHVGO减渣部分脱后原油, 170211CLVGO常压炉前换热网络

13、Slide 19初馏塔闪底油196295度减三中及减三线减渣II脱后原油170211度常二中说明：该加热流程需要管壳式换热器说明：该加热流程需要管壳式换热器10台。其中台。其中316L材质为材质为8台，台，317L材质为材质为2台，价格为台，价格为2600万人民币。不锈钢阀门为万人民币。不锈钢阀门为40个（不含跨线阀门），价格未计算在内个（不含跨线阀门），价格未计算在内常压炉前换热网络Slide 20Summary 总结High efficiency 换热效率高 = Reduce size and number of heat exchangers 减少设备体积，占地面积和设备数量Close tem