一、全装置物料平衡1、物料平衡本设计的处理量为95万吨/年，反应阶段为其末期，每年开工时数按8000小时计算。

入方：①原料油=8000%10010109534⨯⨯⨯=118750公斤/小时=248000%10010954⨯⨯⨯=2850吨/天 ②重整氢=8000%70.210109534⨯⨯⨯=3206公斤/小时=248000%70.210954⨯⨯⨯=77吨/天 出方：①精制柴油=118750×96.95%=115128公斤/小时= 2850×96.95%=2763吨/天②粗汽油=118750×1.52%=1805公斤/小时=2850×1.52%=43吨/天③高分排放气=118750×1.78%=2114公斤/小时=2850×1.78%=51吨/天④低分排放气=118750×0.31%=368公斤/小时=2850×0.31%=8.8吨/天⑤回流罐排放气=118750×2.084%=2475公斤/小时=2850×2.084%=59吨/天⑥溶于水中的硫化氢=118750×0.022%=26公斤/小时=2850×0.022%=0.6吨/天⑦溶于水中的氨气=118750×0.024%=28.5公斤/小时=2850×0.024%=0.7吨/天⑧设备漏损=118750×0.01%=12公斤/小时=2850×0.01%=0.3吨/天 2、化学耗氢量计算①计算杂质脱除率a) 硫脱除率 =18001801800-×100% = 90%b) 氮脱除率 = 26158261-×100% = 77.8%c) 硫醇硫脱除率 = 15115-×100% = 93.3%d) 氧脱除率（以酸度计算）原料油含氧率 =8642.01001656/108.53⨯⨯⨯-×100% = 0.00192%精制油含氧率 = 8595.01001656/1014.03⨯⨯⨯-×100% = 0.0000463%氧脱除率=00192.00000465.000192.0-×100% = 97.58%e) 烯烃饱和率（以溴价计算）烯烃饱和率=5.201.45.20-×100% = 80%②化学耗氢量计算a) 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/T2.34×118750/22.4×10002=25kg/hrb) 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/ T1.26×118750/22.4×10002=13 kg/hrc) 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⨯⨯⨯⨯- = 0.0967 Nm 3/ T0.0967×118750/22.4×10002=1kg/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/T22.96×118750/22.4×10002=243kg/hre) 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/ T6.29×118750/22.4×10002=67kg/hrf) 每脱掉1%的硫醇硫消耗12.5Nm 3H 2/m 3原料油 硫醇硫耗氢量=8642.0100%3.9310155.126⨯⨯⨯⨯- = 0.02 Nm 3/ T0.0202×118750/22.4×10002=0.2kg/hrg) 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 = 10Nm 3/T10.22×118750/22.4×10002=108kg/hr总化学耗氢量=2.34+1.26+0.0967+22.96+6.29+0.0202+10.22=43Nm 3/T =24.81+13.36+1.025+243.44+66.69+0.214+108.36=458 kg/hr重量分数：加氢脱硫：899.45781.24×100% =5.42%加氢脱氮：899.45736.13×100% =2.92%加氢脱氧：899.457025.1×100% =0.22%烯烃饱和：899.45744.243×100% =53.16%芳烃饱和：899.45769.66×100% =14.56%硫醇脱硫：899.457214.0×100% =0.05%加氢裂解：899.45736.108×100% =23.66%3、化学反应放热量a)．加氢脱硫反应放热量=600 kcal/ Nm 3×2.34 Nm 3/T =1404kcal/T 1404 kcal/T×118.75T/hr=166725kcal/hr b)．加氢脱氮反应放热量=600 kcal/ Nm 3×1.26 Nm 3/T =756kcal/T 756kcal/T×118.75T/hr=89775kcal/hr c)．加氢脱氧反应放热量=600 kcal/ Nm 3×0.0967 Nm 3/T =58.02kcal/T58.02kcal/T×118.75T/hr=6890kcal/hrd)．加氢烯烃饱和反应放热量=1260 kcal/ Nm 3×22.96 Nm 3/T =28929.6kcal/T28930kcal/T×118.75T/hr=3435438kcal/hr e)．加氢芳烃饱和反应放热量=540 kcal/ Nm 3×6.29 Nm 3/T =3396.6kcal/T3397kcal/T×118.75T/hr=403394kcal/hr f). 加氢裂解反应放热量=450 kcal/ Nm 3×10.22 Nm 3/T =4599kcal/T4599 kcal/T×118.75T/hr=546131kcal/hr总的反应放热量∑=1404+756+58.02+28930+3397+4599=39144kcal/T=166725+89775+6889.875+3435437.5+403393.75+546131.25=4648352.375kcal/hr重量分数：加氢脱硫：%59.3%100391441404=⨯加氢脱氮：%93.1%10039144756=⨯ 加氢脱氧：%15.0%1003914402.58=⨯烯烃饱和：%95.73%100391446.28929=⨯芳烃饱和：%68.8%100391446.3396=⨯加氢裂解：%76.11%100391444599=⨯4、纯氢平衡表入方：新氢=5.51095%7.27⨯⨯×2×87.68%/8000 = 1022kg/hr10002427.1022⨯=25T/d出方：化学耗氢量=458kg/hr100024899.457⨯=10.99T/d排放耗氢量=5.675.2113×2×80.86% = 525.9kg/hr1000249.525⨯=13T/d溶解耗氢（包括低分排放和回流罐排放）：低分罐=11.18125.368×43.10%×2=18kg/hr回流罐=46.4475.2474×2.03%×2=2. kg/hr溶解耗氢总量∑=17.52+2.26=20kg/hr10002478.19⨯=0.47472T/d机械漏损：入方-出方=1022.27-(457.899+525.9+19.78)=18.691kg/hr100024691.18⨯=0.449T/d重量分数：化学耗氢：27.1022899.457×100%=44.79%排放耗氢：27.10229.525×100%=51.44%溶解耗氢：27.102278.19×100%=1.93%机械漏损：27.1022691.18×100%=1.83%5、硫化氢的物料平衡产生H 2S ：3432%901018001187506⨯⨯⨯⨯-=204kg/hr10002440.204⨯=5T/d排放H 2S ：①高分排放：34%6.05.675.2113⨯⨯=66kg/hrT/d 6.110002434.66=⨯②低分排放：34%55.211.18125.368⨯⨯=18kg/hrT/d 4.010002462.17=⨯③回流罐排放：34%85.446.4475.2474⨯⨯=92kg/hrT/d 2.210002479.91=⨯④水中溶解：26kg/hr （在装置总物料平衡中已计算） T/d 6.0100024125.26=⨯⑤粗汽油中溶解：204.40-（66.34+17.62+91.79+26.125）=2.5kg/hr T/d 06.0100024525.2=⨯重量分数：高分排放：%10040.20466⨯=32.46%低分排放：10040.20418⨯%=8.62%回流罐排放：10040.20492⨯%=44.90%水中溶解：10040.20426⨯%=12.78%粗汽油中溶解：10040.2045.2⨯%=1.24%二、反应器的工艺设计入口温度为320℃，入口压力为4.0Mpa，取塔径为3.4m，出口压力为3.9Mpa，选用固定床轴向冷壁式反应器，已知数据如下：表一在压力为4.0Mpa时，温度与气化率和热焓的对应关系如下：加氢反应器入口温度℃气化率we（%）混合焓（Kcal/kg）226 4.72 186.64266 9.49 217.26310 19.09 254.15359 28.81 295.91374 38.65 311.58表二在不同压力下，气化率与温度和热焓之间的对应关系如下：系统压力P=3.9Mpa P=3.8Mpa P=3.7Mpa P=3.6Mpa气化率we（%）温度℃混合焓（Kcal/kg）温度℃混合焓（Kcal/kg）温度℃混合焓（Kcal/kg）温度℃混合焓（Kcal/kg）4.54 196 166.98 194 165.67 193 165.01 191.5 164.03 9.44 267 218.16 265 216.73 264 216.01 262 215.32 19.00 311 254.67 310 253.9328.68 341 281.62 339 279.8938.47 360 299.9248.38 375 315.31注：物料包括加氢生成油，反应生成气和循环氢图一 3.90Mpa下焓值与温度对应关系图二 3.90Mpa 下气化率与温度对应关系表三不同气化率下的油气平均分子量气化率w e （%）平均分子量10 155 20 160 30 165 40170图三 不同气化率的油气平均分子量1.催化剂装填体积（选空速=2.5h -1）空速=催化剂的体积时的体积油在C 20︒=催V 8000/2.86410957⨯=2.5催V ∴=54.96m 3假设D=3.4m ，则L=2V 4D π催⨯=24.314.396.544⨯⨯=5.06m 2.催化剂的当量直径（所选催化剂为mm 62.1⨯Φ）D p =6×F V =6×3323323106102.12)102.1(4/106)102.1(4/-----⨯⨯⨯⨯+⨯⨯⨯⨯⨯⨯⨯πππ=1.64×310-m 3.循环氢（选氢油比=300） 氢油比=油混合氢V V =2.864/8000/1095V 7⨯混合氢=300混合氢V ∴=41223.1Nm 3 混合氢w =混合氢V /22.4×M =18.64.221.41223⨯=11373.16kg/hr 循环氢w =混合氢w -新氢w =11373.16-3206.25=8166.91kg/hr4.D E =0.335.反应器入口温度下物料的气化率和氢分压作4.0Mpa 下的H m ～t 、e w %～t 图，查得t=320℃时，e w =21%，H m =262.0Kcal/kg 由图可得：当e w =21%时，油气M =160.5g/mol入口2p H =总p ×油气纯氢纯氢m m m +=4.0×油气M e w⨯+⨯11875018.6/16.11373%08.83)18.6/(11373.16=3.06Mpa6.反应器出口温度及气化率根据热量衡算得：（原料油混合氢w w +）入口m H +Q×95%=（原料油混合氢w w +）出口m H(11373.16+118750) ×262.0+39144×118750×310-×95%=（11373.16+118750）出口m H 出口m H =295.94Kcal/kg作t ～H m 、e w %～H m 图，查得出口w e =36.0%，出口t =356℃ 7.出口氢分压反应生成气m =循环氢m +[1-(96.95%+1.52%)]×原料油m=1187500153.091.8166⨯+=9983.785kg/hr由图可得：当e w =36.0%时，油气M =168g/mol出口2pH =总p ×油气原料油反应生成气反应生成气（M e w /%)52.1%95.96m 95.7/m %60.7795.7/m ⨯+⨯+⨯=3.9×168%0.369847.011875095.7/785.9983%60.77)95.7/(9983.785⨯⨯+⨯=2.52Mpa8..气体密度v ρt =(进口t +出口t )/2=(320+356)/2=338℃w e =(进w e +出w e )/2=(21%+36%)/2=28.5%mol g /25.164)105.28()1020/()155160(155M =-⨯--+=气w =混合氢w +原料油w ×w e =11373.16+118750×28.5%=45216.91kg/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 +=[18.611373.16+25.164%5.28187501⨯]×22.4×869.995.31⨯×273273338+ =2631.72m 3/hr v ρ=气气V w =72.263191.45216=17.18kg/m 39.空塔线速u假设D=3.4m ，则S==(π/4)D 2=9.075m 2 u=S气V =3600075.972.2631⨯=0.081m/sec10.混合物粘度查分子量为164.25、温度为338℃下，石油馏分蒸汽粘度为i z =0.0082厘泊Tr=）（）（K c K T T =40.182.33273338=+ Pr=05.3297.195.3Pc P == 根据Tr 与Pr 氢的粘度图得2iH z =0.013厘泊[2]原料油原料油混合氢纯氢原料油混合氢油气）（）（M e m 8308.0118.6m m e 1m m M ww ⨯+-⨯--+=34.197%5.281187508308.0118.611373.162%08.8318.611373.16%5.28111875016.13731⨯+-⨯⨯⨯--⨯+=）（）（ =193.052H 粘度：i y 总p p 2H =25.164%5.2811875018.616.11373%08.8318.616.11373⨯+⨯=0.747 混z =∑∑0.5iii0.5ii my z my =5.05.05.05.005.193747.012747.00082.005.193747.01013.02747.0⨯-+⨯⨯⨯-+⨯⨯）（）（ =9.31×310-厘泊 11.求hv G =w e m m ⨯+原料油混合氢=11373.16+118750×28.5%=45216.91kg/hrL G =）（原料油w e 1m -=118750×(1-28.5%) =84906.25kg/hr L G /v G =84906.25/45216.91=1.878 v G =45216.91kg/hr=24.34/2048.091.45216⨯⨯π=1020.5磅/2尺·hr 根据v G 与L G /v G 关系图查得：h=0.181.13p 1.09.19.05])3.2/1(367.0[h E 103.6h D h z u L p p v ++⨯-⨯⨯=∴-）（ρΔ混 =1.133239.19.05])3.2/18.01(1064.1318.067.0[18.033.01000/1021.907.018.17103.6+⨯⨯⨯+⨯-⨯⨯⨯⨯⨯---）（）（ =0.1034Pa/m12.检验 ①=LpΔ0.1034Pa/m ，在0.023～0.115Pa/m 范围内 ②15.14.306.5D L >==③=⨯=L Lpp ΔΔ0.1034×5.06=0.523 kg/cm 2<0.84kg/cm 完全符合要求。