柴油加氢精制一．物料平衡1. 全装置物料平衡本设计催化柴油处理量为100万吨/年，反应阶段为其末期，年开工时数为8000小时。

装置总物料平衡表 （年开工时数以8000小时/年）注: 粗汽油包括0.03 的溶解气在内由∑入方=∑出方，得设备漏损为0.01% < 1%.2. 化学耗氢量 1) 杂质脱除率a) 硫脱除率 =18001801800-×100% = 90%b) 氮脱除率 =26158261-×100% = 77.78% c) 氧脱除率（以酸度计算） 原料油含氧率 =8642.01005616108.53⨯⨯⨯⨯-×100% = 0.00192%精制油含氧率 = 8595.010056161014.03⨯⨯⨯⨯-×100% = 0.0000463%氧脱除率=00192.00000465.000192.0-×100% = 97.58%d) 烯烃饱和率（以溴价计算）烯烃饱和率=1.45.20-×100% = 80%2) 化学耗氢量a) 脱硫耗氢每脱掉1%的硫消耗12.5Nm 3H 2/m 3原料油加氢脱硫耗氢量=8642.0100%901018005.126⨯⨯⨯⨯- = 2.34 Nm 3/T 原料油2.34×125000/22.4×10002=26.152kg/hrb) 脱氮耗氢每脱掉1%的氮消耗53.7Nm 3H 2/m 3原料油加氢脱氮耗氢量=8642.0100%8.77102617.536⨯⨯⨯⨯- = 1.26 Nm 3/ T 原料油1.26×125000/22.4×10002=14.078kg/hrc) 脱氧耗氢每脱掉1%的氧消耗44.6Nm 3H 2/m 3原料油加氢脱氧耗氢量=8642.0100%6.971092.16.445⨯⨯⨯⨯- = 0.0966Nm 3/ T 原料油0.0966×125000/22.4×10002=1.078kg/hrd) 烯烃饱和耗氢量烯烃饱和耗氢量=（20.5-4.1）×10×22.4/160 = 22.96 Nm 3/T 原料油22.96×125000/22.4×10002=256.25kg/hre) 芳烃饱和饱和1%的芳烃消耗5.0Nm 3H 2/m 3原料油芳烃饱和耗氢量=8642.0568.05.411.43⨯⨯-）（=6.29 Nm 3/ T 原料油6.29×125000/22.4×10002=70.254kg/hrf) 加氢裂解耗氢量原料油裂解程度为3%，每裂解1分子原料，消耗3分子氢加氢裂解耗氢量=34.197%31000⨯×3×22.4 = 10.22Nm 3/T 原料油10.22×125000/22.4×10002=114.017kg/hr各类加氢反应的耗氢量汇总表3. 反应放热a) 加氢脱硫反应放热量=600 kcal/ Nm 3×2.34 Nm 3/T =1405.92kcal/T1405.92 kcal/T×125T/hr=175740kcal/hrb) 加氢脱氮反应放热量=600 kcal/ Nm 3×1.26 Nm 3/T =756.84kcal/T756.84kcal/T×125T/hr=94605kcal/hrc) 加氢脱氧反应放热量=600 kcal/ Nm 3×0.0966 Nm 3/T =57.95kcal/T57.95kcal/T×125T/hr=7243.5kcal/hrd) 加氢烯烃饱和反应放热量=1260 kcal/ Nm 3×22.96 Nm 3/T =28929.6kcal/T28929.6kcal/T×125T/hr=3616200kcal/hre) 加氢芳烃饱和反应放热量=540 kcal/ Nm 3×6.29 Nm 3/T =3399.19kcal/T3399.19kcal/T×125T/hr=424899kcal/hrf) 加氢裂解反应放热量=450 kcal/ Nm 3×10.22 Nm 3/T =4597.16kcal/T4597.16 kcal/T×125T/hr=574644.38 kcal/hr反应放热计算汇总表4. 纯氢消耗量汇总a) 入方：新氢=5.510100%7.27⨯⨯×2×87.68%/8000 = 1076.073kg/hr100024073.1076⨯=25.83T/db) 出方：化学耗氢量=481.829kg/hr100024829.481⨯=11.56T/d排放耗氢量=5.62225×2×80.86% = 553.58kg/hr10002458.553⨯=13.29T/d溶解耗氢（包括低分排放和回流罐排放）：低分罐=11.185.387×43.10%×2=18.444kg/hr回流罐=46.442605×2.03%×2=2.379kg/hr∑=18.444+2.379=20.823kg/hr100024823.20⨯=0.4998T/d机械漏损=1076.073-(481.829+553.58+20.823)=19.841kg/hr100024841.19⨯=0.476T/d加氢精制装置纯氢消耗量汇总表5. 硫化氢平衡a) 入方：3432%901018001250006⨯⨯⨯⨯-=215.16kg/hr 10002416.215⨯=5.16T/db) 出方：高分排放：34%6.05.62225⨯⨯=69.83kg/hr T/d 68.110002483.69=⨯ 低分排放：34%55.211.185.387⨯⨯=18.55kg/hr T/d 45.010002455.18=⨯回流罐排放：3485.446.442605⨯⨯=96.62kg/hr T/d 32.210002462.96=⨯水中溶解：27.50kg/hr T/d 66.010002450.27=⨯漏损：215.16-（69.83+18.55+96.62+27.50）=2.66kg/hr氢装置内硫化氢平衡表二．反应器设计入口温度为280℃，入口压力为4.0Mpa ，出口压力为3.9Mpa ，已知数据如下：加氢反应器入口注：物料包括原料油，新氢和循环氢注：物料包括加氢生成油，反应生成气和循环氢注：气相油平均分子量图1 不同气化率的油气平均分子量图2 3.90Mpa下焓值与温度对应关系图3 3.90Mpa下气化率与温度对应关系1. 催化剂装填体积空速=催化剂的体积时的体积油在C 20︒=催V 8000/2.864101007⨯=2.5 催V ∴=57.86 m 32. 催化剂当量直径所选催化剂为RN-1催化剂（mm 62.1⨯Φ）D p =6×F V =6×3323323106102.12)102.1(4/106)102.1(4/-----⨯⨯⨯⨯+⨯⨯⨯⨯⨯⨯⨯πππ=1.6364×310-m 3. 循环氢和混合氢流量氢油比=油混合氢V V =2.864/8000/10100V 7⨯混合氢=300混合氢V ∴=43392.73Nm 3/hr 混合氢w =混合氢V /22.4×M =18.64.2243392.73⨯=11971.74kg/hr 循环氢w =混合氢w -新氢w =11971.74-3375=8596.74kg/hr4. 入口氢分压作4.0Mpa 下的H m ～t 、e w %～t 图，查得t=320℃时，e w =20.5%，H m =263Kcal/kg 由图可得：当e w =20.5%时，油气M =160.25g/mol入口2p H =总p ×油气纯氢纯氢m m m +=4.0×油气M e w⨯+⨯12500018.6/74.11971%08.83)18.6/(11971.74=3.070Mpa5. 反应器出口温度计算根据热量衡算得：（原料油混合氢w w +）入口m H +Q=（原料油混合氢w w +）出口m H(11971.74+125000) ×263+4.893×106=（11971.74+125000）出口m H 出口m H =298.72Kcal/kg作t ～H m 、e w %～H m 图，查得出口w e =37.3%，出口t =358℃6. 出口氢分压反应生成气m =混合氢m +[1-(96.95%+1.49%)]×原料油m=12305074.11971125000-+=13921.74kg/hr由图可得：当e w =37.3%时，油气M =168.65g/mol出口2p H =总p ×油气原料油反应生成气反应生成气（M e w /%)49.1%95.96m 95.7/m %60.7795.7/m ⨯+⨯+⨯=3.9×65.168%3.3712305095.7/74.13921%60.77)95.7/(13921.74⨯+⨯=2.619Mpa7. 气体密度t =(进口t +出口t )/2=(358+320)/2=339℃w e =(进w e +出w e )/2=28.9%mol g /45.164M =气w =混合氢w +原料油w ×w e =11971.74+125000×28.9%=48096.74kg/hr 气V =[混合氢混合氢M w +油气原料油M e w w⨯]×22.4×869.995.31⨯×273273t +=[18.611971.74+45.164%9.28250001⨯]×22.4×869.995.31⨯×273273339+=2778.34 m 3/hrv ρ=气气V w =17.31 kg/m 38. 混合物黏度油气原料油混合氢纯氢原料油混合氢）油气（包含氢气中杂质）（M e m 8308.0118.6m m e m m M ww ⨯+-⨯-⨯+=5.4164%.9281250008308.0118.611971.742%08.8318.611971.74289.01250004.719711⨯+-⨯⨯⨯-⨯+=）（=81.978 mol g /查81.978 mol g /，温度为339℃下，石油馏分蒸汽粘度为i z =0.0145厘泊【1】Tr=）（）（K c K T T=43.182.33273339=+Pr=045.3297.195.3Pc P == 根据Tr 与Pr 氢的粘度图得2iH z =0.0143厘泊[1]2H 摩尔分数：i y =总p p 2H =45.164%9.2812500018.674.11971%08.8318.674.11971⨯+⨯=0.746 混z =∑∑0.5iii0.5ii my z my =5.05.05.05.0978.81746.012746.00145.0978.81746.010143.02746.0⨯-+⨯⨯⨯-+⨯⨯）（）（ =0.0144厘泊 9. 空塔线速取D=3.6m ，则u=S气V =23.6π25.034.2778⨯⨯=288.77 m/hr =0.0802 m/s 10. 液体滞留量v G =w e m m ⨯+原料油混合氢=11971.74+125000×28.9%=48096.74kg/hrL G =）（原料油w e 1m -=125000×(1-28.9%)=88875kg/hr L G /v G =1.8478 v G =48096.74kg/hr=25.34/2048.048096.74⨯⨯π=1085.00磅/2尺·hr 根据v G 与L G /v G 关系图查得：h=0.1551.13p 1.09.19.05])3.2/1(367.0[h E 103.6h D h z u L p p v ++⨯-⨯⨯=∴-）（ρΔ混 1.1331.039.19.05])3.2155.01(10636.13155.067.0[155.033.0100107.00802.031.17103.6+⨯⨯⨯+⨯-⨯⨯⨯⨯⨯=---）（）（=0.1085Pa/m11. 校核①=Lp Δ0.1085Pa/m ，在0.023～0.115Pa/m 范围内②17.16.301.6D L >== ③=⨯=L L pp ΔΔ0.1085×6.01=0.6519kg/cm 2<0.84kg/ cm 2，符合要求。