典型装置焦化炉操作状况剖析

1、2. 燃料组成对对流室传热效果的影响表21燃料组成项目单位石家庄沧州塔河金山胜华xx史口天津石化燃料组成甲烷v%38.249.8856.90644.8717.6732.7560.8719.78乙烷v%18.4345.4520.59115.928.5812.05208.55乙烯v%1.7430.611.8232.9349.5915.54.40丙烷v%14.4433.191.0648.1922.810.81.911.66丙烯v%3.15820.760.6014.4842.733.81.653.91丁烷v%7.960.380.0842.536.330.50.135.64丁烯v%2.1931.390.

2、3102.3040.750.8501.19戊烷v%2.7980.910.4430.3080.3000.95戊烯v%000.00000000氢气v%9.518.2618.1798.65641.5322.710.4922.96硫化氢v%0005.0680000.015一氧化碳v%00.92000.43000.0016氧气v%01.802.2211.81.99503.1429二氧化碳v%09.4100.2920.671.5505.7916氮气v%1.53127.0402.2216.87.505016.4232水v%0000000.550合计v%100100100100100100100100燃料低热

3、值kj/kg4697226786502934316043283413974927833449理论空气用量kg/kgf15.838.6416.9814.4613.9913.4516.6510.99过剩空气系数1.251.251.251.251.251.251.251.25实际空气用量kg/kgf19.7810.8021.2218.0717.4916.8220.8113.74表22操作条件项目单位数值备注辐射进料量kg/h63670双路介质入炉温度307辐射出口温度493.5辐射出口压力mpa0.38绝压一次注水量kg/h353.5一次注水位置1二次注水量kg/h131.5二次注水位置31注水温度

4、364注水压力mpa1.4绝压汽化分率m%100空气入炉温度194预热后过剩空气系数1.25表23 不同燃料组成对对流传热系数的影响燃料来源项目单位石家庄沧州塔河金山胜华xx史口天津石化辐射入口压力mpa1.18961.18961.18951.18961.18881.18881.18951.1895燃料用量nm3/hr863.915491330.61087.614431406.31250.31354kg/hr11021941103511941192124210541556烟气流量kg/hr2289422915229942278322039221312299222935单耗kgeo/t渣油19.

5、4119.5119.5219.3419.3519.2919.4819.52炉膛温度778.23778.23778.21778.21778.78778.78778.2778.21烟气经油换热后温度434.2435437.6435.4432.4432.5437.3436.3对流转辐射温度360.8360.7361.3360.7359.93360361.2361渣油段传热量kw2664.22659.326892659.32611.82615.226842674.1管外综合对流传热系数w/m2c19.40919.40119.46619.37919.16819.1919.45919.429管内综合对流传

6、热系数w/m2c562.852562.852562.852562.852562.852562.852562.852562.852总对流传热系数w/m2c18.618.618.6618.5818.3818.418.6518.62说明炉结构、操作条件及原料油物性数据均取自石家庄2005年8月数据3. 辐射进料馏程对关键工艺参数的影响表31辐射进料馏程汇总表（11种）大庆减渣进料馏程温度收率%20密度51095.670.9969总计100.9939辽河循环进料馏程温度收率%20密度51088.79520.9969总计100.9912济南循环进料馏程温度收率%20密度51086.50.9969总计10

7、0.9873荆门循环进料馏程温度收率%20密度51085.780.9969总计100.9886长岭进料馏程温度收率%20密度51075.0891.0468总计1001.0217石家庄进料馏程温度收率%20密度510751.0135总计100.99995沧州循环进料馏程温度收率%20密度51072.620.9969总计100.9765统计14进料馏程温度收率%20密度510661.027213总计1001.0010锦西进料馏程温度收率%20密度51057.550.9969总计100.9692稠油厂进料馏程项目收率%20密度51057.251.0011总计1000.9654xx进料馏程温度收率%2

8、0密度51051.790.974总计1000.9409表32不同辐射进料馏程计算操作参数项目单位数值备注渣油处理量kg/hr51400全炉t/d1234万吨/年41.12循环比0.123入辐射室温度346.5出炉温度494.2出炉压力mpa0.35绝压空气入炉温度179.4过剩空气系数1.19一次注水量kg/h343.2单路一次注水位置1汽化分率m%100注水温度225.1二次注水量kg/h205.3单路二次注水位置31汽化分率m%100注水温度255.7辐射室相对散热0.03表33不同辐射进料馏程计算燃料组成项目数值v%备注甲烷42.177乙烷17.236乙烯1.844丙烷11.995丙烯3

9、.274丁烷7.035丁烯1.98戊烷2.025戊烯0氢气6硫化氢0一氧化碳0氧气1.26445二氧化碳.158氮气5.0115水0表34辐射进料馏程对关键工艺参数的影响汇总表项目单位大庆减渣辽河济南荆门长岭石家庄沧州统计14锦西稠油厂xxmaxmin循环油管内停留时间s8784.683.9384.3384.1584.7483.6384.4284.3682.8183.2487.0082.81430以上停留时间s30.4729.2528.1628.8029.8030.2228.1230.6429.4828.1427.7430.6427.74管内裂化转化率m%5.995.885.555.685.8

10、45.895.345.935.715.405.275.995.27管内缩合转化率m%0.0890.0880.0820.0840.0860.0870.0780.0870.0840.0790.0770.090.08出口汽化分率m%8.7615.6717.7418.5729.5429.6931.6438.8236.7847.1552.5652.568.76最大表观流速m/s22.8525.0026.3426.1731.6830.3531.8134.7647.1738.5139.5947.1722.85最高边界底层温度505503503503501501501500500499499505499最高管

11、外壁温度510508508508506507506506505505504510504炉膛温度739744743744747751747753755753755755739平均热强度kw/m220.2520.8520.6620.8321.1821.6321.1921.8822.0721.8022.0322.0720.25生焦反应焦化炉给热kj/kg279290284289306313297323319312312323279反应行程长度m277279277279291291282296291288285296277标油消耗kgeo/t渣油20.9221.6421.4121.6122.0322.

12、5822.0522.8923.1222.7923.0723.1220.92介质总吸热kw4237436343224358443145274434457946194562461046194237生焦反应总给热kw2233232222782320245525082384258725592503250425872233生焦反应总给热/介质总吸热52.6953.2352.6953.2355.4155.4153.7856.4955.4154.8654.3256.4952.69炉内反应总吸热kw421512446486614634439637498440363637363炉内反应总吸热/介质总吸热9.94

13、11.7410.3311.1513.86149.913.9210.799.647.8714.007.87压降mpa0.72640.76940.79170.7870.84780.830.850.8720.88560.91150.91740.920.73说明1、操作数据取自石家庄焦化炉-2，2005年6月17日10：002、生焦反应总给热、介质总吸热、炉内反应总吸热均为单程数据4. 12集总动力学常数对关键工艺参数的影响图41a 12集总动力学常数库表41 12集总动力学常数计算操作参数燃料性质项目单位数值备注渣油处理量kg/hr51400全炉t/d1234万吨/年41.12循环比0.123入辐射

14、室温度346.5出炉温度494.2出炉压力mpa0.35空气入炉温度179.4过剩空气系数 1.19一次注水量kg/h343.2单管程一次注水位置 1汽化分率m%100注水温度225.1二次注水量kg/h205.3单管程二次注水位置 31汽化分率m%100注水温度255.7辐射室相对散热 0.03项目数值v%甲烷42.177乙烷17.236乙烯1.844丙烷11.995丙烯3.274丁烷7.035丁烯1.98戊烷2.025戊烯0氢气6硫化氢0一氧化碳0氧气1.26445二氧化碳0.158氮气5.0115水0表42 12集总动力学常数对关键工艺参数的影响汇总表项目单位7种混合10种混合11种混合

15、济南减渣沙特轻油特例原油辽河原油maxmin循环油管内停留时间s85.1484.4984.4284.4884.4384.4886.9586.9584.42430以上停留时间s27.2330.6130.6429.0930.6329.0930.2330.6427.23管内裂化转化率m%2.556.355.934.745.714.734.576.352.55管内缩合转化率m%0.110.180.090.760.180.760.530.760.09最大表观流速m/s39.0839.2538.8237.9138.6237.9049.9849.9837.90出口汽化分率m%35.7435.1034.763

16、4.4334.6734.4345.8545.8534.43最高边界底层温度500500500500500500498500498最高管外壁温度504506506505509505504509504炉膛温度738755753748752748747755738平均热强度kw/m220.1022.0921.8821.2421.7721.2321.1122.0920.10生焦反应焦化炉给热kj/kg276326323304321304302326276反应行程长度m276.5296.45296.45287.9296.45287.9287.9296.45276.50标油消耗kgeo/t渣油20.742

17、3.1422.8922.1122.7522.121.9523.1420.74介质总吸热kw420646224579444545554443441746224206生焦反应总给热kw221626112587243925732437242326112216生焦反应总给热/介质总吸热52.6956.4956.4954.8656.4954.8654.8656.4952.69炉内反应总吸热kw252.5679.6637.3508.8617.5507.8439.7679.6252.5炉内反应总吸热/介质总吸热614.713.9211.4513.5611.439.9514.706.00压降mpa0.8720

18、.8750.8720.8700.8720.8700.8940.8940.870说明1、操作数据取自石家庄焦化炉-2，2005年8月5日2、生焦反应总给热、介质总吸热、炉内反应总吸热均为单程数据5. 炉膛结构尺寸对关键工艺参数的影响表51炉膛结构尺寸对关键工艺参数的影响操作参数项目单位单面双面备注减渣进料量万吨/年38.2076.41单炉t/d11462292kg/h4775595510循环比 0.4240.424入辐射温度371.5371.5出炉温度500500出炉压力mpa0.370.37绝压空气入炉温度208208换后温度过剩空气系数 1.241.24 一次注水量kg/h607.5607.

19、5单路一次注水位置 11汽化分率00注水温度m%226226辐射室相对散热%0.030.03表52炉膛结构尺寸对关键工艺参数的影响物性燃料组成温度收率%20密度510751.0135项目数值v%甲烷56.9乙烷20.59乙烯1.82丙烷1.06丙烯0.6丁烷0.08丁烯0.31戊烷0.44戊烯0氢气18.18硫化氢0一氧化碳0氧气0二氧化碳0氮气0水0表53不同加热炉尺寸项目单位安庆201安庆201长岭稠油厂海科石家庄塔河克拉玛依高桥金山济南长岭武石化备注底部高mm6474835077507400619684735640674062755958575764445640斜顶高mm16731829

20、1237.51884128512000000000底部宽mm4581530646004960455646305880336526162616262433655880上部宽mm17431836182023181246216258801420026162616262433655880炉长mm848014398144801440284801140218512243702396018199181991883418000火嘴个数mm621321321326282128188168128128128128火盆间距mm90013001000120018001300810800875800800800810火

21、盆尺寸mm350370460470520460720/480660/432508/419660/432660/432660/432720/480长/宽辐射炉管总根数根502442402402502422224244244244244244264遮蔽管根数根4231212242420000000斜顶管根数根109781060000000下部炉管根数根32323128323222242424242426炉管长mm900015000150001500090001200017500229952299517464174661750017500直管长管内径mm73107107107731078210710

22、397.1897.1897.18122.24di，扩管前管外径mm8912712712789127102127127114.3114.3114.3141.3do，扩管前管心距mm178250250250178250203215215203.2203.2203.2203s1，扩管前管底间距mm5006006005005000420406425425417406420中心距底转油线一段水平管长mm01000828122501225/中间墙高mm11001500196902.4924903350409141543889040913350反射墙转油线二段垂直管长mm080677725720602200

23、/转油线三段水平管长mm01000828122501950/单程总管长m450660600600424504385551.88551.88426.792419.184452.016455单程总管长传热面积m2251.64526.66478.78478.78237.10402.17493.48880.76880.76613.02602.09649.25807.91表54不同加热炉相同操作条件相同物性计算结果汇总项目单位单面焦化炉双面焦化炉安庆201安庆202长岭稠油厂海科石家庄塔河克拉玛依高桥金山济南长岭双面武石化循环油管内停留时间s52.183.7873.1473.1451.966.2731.

24、0848.5548.7634.2534.2434.4138.07430以上停留时间s25.4740.8634.3834.325.4630.3613.3721.5221.5714.4414.4514.4816.92管内裂化转化率m%8.46211.6489.7889.7798.4578.6073.5435.9285.8923.8533.8473.8565.075管内缩合转化率m%0.1430.1890.1580.1580.1430.1390.0570.0960.0950.0620.0620.0620.084出口汽化分率m%31.8934.49732.94332.93431.88531.96427

25、.82929.76929.73628.0828.07528.08229.087最大表观流速m/s52.3035.6434.5134.4452.2734.1445.4032.6634.6036.7036.6636.6525.63最高边界底层温度514507507507514508508507507508508508509最高管外壁温度523512513513523514517512513515514514514炉膛温度923775788786927802727646678722723711694平均热强度kw/m247.1823.4524.7224.8547.1726.4938.4522.452

26、2.8931.8831.8730.7924.28生焦反应焦化炉给热kj/kg379413389389379370308327339312312297314反应行程长度m271418373371271331236345351258258254276标油消耗kgeo/t渣油35.4832.3831.631.5235.6331.0526.2825.6526.3926.0726.0825.8225.68介质总吸热kw5593592857135711559255435018523852515000499849985043生焦反应总给热kw357839053676367535773493291030873

27、2032950294928042969生焦反应总给热/介质总吸热63.9765.8864.3464.3463.9763.0157.9858.9460.9959.0159.0156.1158.86炉内反应总吸热kw104714141202120110461066455748744494493494644炉内反应总吸热/介质总吸热18.7123.8521.0521.0418.719.239.0814.2814.169.889.879.8912.77压降mpa3.21431.22961.15181.15183.20951.11741.34990.72660.82010.85220.85260.852

28、40.4313说明生焦反应总给热、介质总吸热、炉内反应总吸热均为单程数据表55不同加热炉相同操作条件相同物性计算结果对比项目单位单双面综合单面焦化炉双面焦化炉平均maxmin平均maxmin平均maxmin循环油管内停留时间s51.5183.7831.0866.7283.7851.9038.4848.7631.08430以上停留时间s23.6640.8613.3731.8140.8625.4616.6821.5713.37管内裂化转化率m%6.8311.653.549.4611.658.464.575.933.54管内缩合转化率m%0.110.190.060.160.190.140.070.1

29、00.06出口汽化分率m%30.5234.5027.8332.6934.5031.8928.6729.7727.83最大表观流速m/s37.8152.3025.6340.5552.3034.1435.4745.4025.63最高边界底层温度508514507509514507508509507最高管外壁温度515523512516523512514517512炉膛温度762927646833927775700727646平均热强度kw/m230.5047.1822.4532.3147.1823.4528.9438.4522.45生焦反应焦化炉给热kj/kg3484132973874133703

30、16339297反应行程长度m309418236339418271282351236标油消耗kgeo/t渣油29.2035.6325.6532.9435.6331.0526.0026.3925.65介质总吸热kw535659284998568059285543507852514998生焦反应总给热kw329039052804365139053493298232032804生焦反应总给热/介质总吸热61.2665.8856.1164.2565.8863.0158.7060.9956.11炉内反应总吸热/介质总吸热15.5823.859.0820.4323.8518.7011.4214.289.0

31、8压降mpa1.30463.21430.43131.84573.21431.11740.84071.34990.4313综合结果为6个单面焦化炉和7个双面焦化炉汇总6. 不同焦化炉的关键工艺参数表61不同焦化炉对比计算燃料组成项目单位数值备注甲烷v%42.177乙烷v%17.236乙烯v%1.844丙烷v%11.995丙烯v%3.274丁烷v%7.035丁烯v%1.98戊烷v%2.025戊烯v%0氢气v%6硫化氢v%0一氧化碳v%0氧气v%1.26445二氧化碳v%0.158氮气v%5.0115水v%0表62不同焦化炉对比计算物性温度收率%20密度510751.0135表63不同加热炉操作条件

32、项目单位安庆201安庆201长岭稠油厂海科石家庄塔河克拉玛依高桥金山济南长岭武石化备注减渣进料量kg/h14030781004240047755286605140015666.7305004375015094.5355002690015625全炉循环比 0.140.140.230.420.30.1230.80.250.210.340.2270.12进料入辐射温度350340.15390371.5384346.5378384380397.65391370365全炉用量出炉温度491.42493.2495500495494.2494496500498.87497500496进料压力mpa1.22931.76251.80021.53452.0731.181.41271.06981.4641.10521.42280.9940.583出炉压力mpa0.450.4830.550.