7-1附录一物料说明书

1、目录1234总论. - 1 -物料衡算目的 . - 1 -物料衡算方法 . - 1 -各项目核算 . - 2 -4.14.24.34.44.5物料衡算任务. - 2 -烟气脱硫工段物料衡算. - 2 -碳铵冷却结晶工段 . - 7 -牛磺酸工段. - 17 -硫酸铵精制工段. - 26 -56总项目核算. - 36 -硫元素在全厂的流向分析 . - 38 -6.16.26.36.46.5脱硫工段. - 38 -碳铵冷却结晶工段 . - 39 -牛磺酸工段. - 39 -硫酸铵精制工段. - 39 -结论 . - 39 -1 总论本项目拟为吉林建龙钢铁厂的烧结烟气设计一套深度脱硫并予以化利用的装

2、置。烟气脱硫工段采用氨法脱硫，牛磺酸工段采用环氧乙烷-亚硫酸铵法。牛磺酸年产 6800 吨，生产过程中的副氮气和的混合气、碳铵和硫酸铵。这些为我们的工艺产生经济效应。在已确定化学生产工艺和流程后，由定性阶段转向定量阶段，通过对整个生产系统、生产车间，以及部分重要的生产单元进行物料衡算计算出主、副的产量，原材料的消耗定额、“三废”排放量及组成，以及收率等各项经济技术指标，从而定量地评述初步设计所选择的工艺路线、生产方法及工艺流程在经济上是否合理，技术上是否先进，为后阶段的设计提供数据。2 物料衡算目的工艺设计中，物料衡算是在工艺流程确定后进行的。目的是根据原料与之间的定量转化关系，计算原料的消耗

3、量，各种中间、和副的产量，生产过程中各阶段的消耗量以及组成，进而为热量衡算、其他工艺计算及设备计算打基础。对于已有装置，物料衡算可以弄清原料的来龙去脉，找出生产中的薄弱环节，为改进生产、完善管理提供可靠的依据和明确方向，并可作为检查原料利用率及三废处理完善程度的一种3 物料衡算方法工艺设计中，物料衡算是在工艺流程确定后进行的。目的是根据原料与。之间的定量转化关系，计算原料的消耗量，各种中间、和副的产量，生产过程中各阶段的消耗量以及组成，进而为热量衡算、其他工艺计算及设备计算打基础。物料衡算是以质量守恒定律为基础对物料平衡进行计算。物料平衡是指“在时间内进入系统（体系）的全部物料质量必定等于离开

4、该系统的全部物料质量再加上损失掉的和积累起来的物科质量”。物料衡算通式如式：G 投入= G+ G 回收+ G 流失式中：G 投入投入系统的物料总量；G系统产出的和副总量；G 流失系统中流失的物料总量；G 回收系统中回收的物料总量。其中量应包括和副：流失量包括除、副及回收量以外各种形式的损失量，污染物排放量即包括在其中。系统中物料衡算一般表达式为：系统中的积累=输入-输出+生成-消耗式中，生成或消耗项是由于化学反应而生成或消耗的量；积累量可以是正值，也可以是负值，当系统中积累量不为零时称为非稳定状态过程；积累量为零时， 称为稳定状态过程。稳定状态过程时，可以简化为：输入=输出-生成+消耗对无化学

5、反应的稳定过程，又可表示为：输入=输出物料衡算包括总质量衡算、组分衡算和元素衡算。4 各项目核算从原料入厂到输出，其工艺路线可分为如下 4 个工段：（1） 烟气脱硫工段；（2） 碳铵冷却结晶工段；（3）牛磺酸工段；（4）硫酸铵精制工段。4.1 物料衡算任务对于本厂，工艺采取年开工 300 天（7200 小时）的连续操作，其中一年内的四五周（约30 天）用于固定的停车设备检修及紧急情况处理。物料衡算的主要任务在于：（1） 确定牛磺酸的实际产量以及质量指标；（2） 确定氨水、环氧乙烷等原料的循环量以及损失率等指标；（3） 确定工艺中的“三废”排放量等公共经济指标；（4）各主要单元过程的物料衡算，并

6、指导工艺设备的确定；（5）汇总全流程物料衡算，数据用于完成物料流程图等后续设计任务。4.2 烟气脱硫工段物料衡算图 4-1 烟气脱硫工艺示意图由工艺示意图可知，烟气脱硫工段有换热器、脱硫塔等重要单元过程，需要对它们进行物料衡算。表 4-1 E0101 换热器前后物流结果表项目进料流股出料流股温度67.7207.0937.093气相分率00摩尔流量 kmol/hr8374.418374.41表 4-2 E0102 换热器前后物流结果表项目进料流股出料流股温度242.5447.0937.093气相分率11摩80509.249224.1-181.301-201.207H2O3500.843500.8

7、4150000150000166.158159.758-522.212-529.084H2O134990134988N20.000.00SO20.000.00CO20.000.00H+tracetraceOH-9.87610.969HCO3-0.000.00NH3149990.114989NH4+10.47411.633HSO3-0.000.00SO32-0.000.00表 4-3 E0103 换热器前后物流结果表表 4-4 T0101A 脱硫塔前后物流结果表项目进料流股进料流股出料流股出料流股温度204446.465.37.0937.0937.0937.093气相分率0101摩尔流量kmol

8、/hr8374.41133107915.8613172.5质量流量kg/hr150000404193168816385377体积流量cum/hr159.75849224.1149.90852049.3-529.084-201.207-570.212-160.079项目进料流股出料流股温度242.5447.0937.093气相分率11摩80509.249224.1-181.301-201.207H2O3500.843500.84N2310144310144SO21832.461832.46CO288715.588715.5N2310144310144SO21832.461832.46CO2887

9、15.588715.5表 4-5 T0101B 脱硫塔前后物流结果表项目进料流股进料流股出料流股出料流股温度46.44446.145.67.0937.0937.0937.093气相分率0110摩尔流量kmol/hr7915.861331013349.27908.55质量流量kg/hr168816404193405140167870体积流量cum/hr149.90849224.149705.4148.812-570.212-201.207-204.269-567.151组分流量kg/hrH2O1198543500.843319.88120609N29.1513101443101458.677SO

10、2trace1832.460.001trace组分流量kg/hrH2O1349883500.841198547909.4N20.003101449.151310135SO20.001832.46tracetraceCO20.0088715.596.21963647.5H+trace0.00trace0.00OH-10.9690.000.0380.00HCO3-0.000.0034622.30.00NH3149890.00680.5913684.58NH4+11.6330.0011263.90.00HSO3-0.000.0013.460.00SO32-0.000.002276.830.00表 4

11、-6 烟气脱硫工段总物料衡算项目进料流股出料流股流股信息稀氨水烟气 1烟气 2脱硫气 1脱硫气 2氨法脱硫残余液温度67.7242.5242.565.346.145.67.0937.0937.0937.0937.0937.093气相分率011110摩尔流量 kmol/hr8374.41133101331013172.513349.27908.55150000404193404193385377405140167870166.15880509.280509.252049.349705.4148.812-522.212-181.301-181.301-160.079-204.269-567.151

12、H2O1349903500.843500.847909.43319.88120609N20.003101443101443101353101458.677SO20.001832.461832.46trace0.001traceCO20.0088715.588715.563647.59138290.848H+trace-0.000.00traceOH-9.876-0.000.000.029HCO3-0.00-0.000.0030932.8CO296.21988715.59138290.848H+trace0.000.00traceOH-0.0380.000.000.029HCO3-34622.3

13、0.000.0030932.8NH3680.5910.00293.164447.076NH4+11263.90.000.0011200.7HSO3-13.460.000.0033.105SO32-2276.830.000.004547.554.3 碳铵冷却结晶工段图 4-2 碳铵冷却结晶工艺示意图由工艺示意图可知，碳铵冷却结晶工段有反应器、闪蒸罐、换热器和结晶器等重要单元过程，需要对他们进行物料衡算。表 4-7 E0201 换热器前后物流结果表项目进料流股出料流股温度45.6901.0131.013气相分率00摩尔流量 kmol/hr7908.558401.04167870167870148.

14、84385578-567.168-530.562H2O120609129481N28.6778.677NH3149990.1-3684.58293.164447.076NH4+10.474-0.000.0011200.7HSO3-0.00-0.000.0033.105SO32-0.00-0.000.004547.55表 4-8 R0201 反应器前后物料结果表项目进料流股出料流股温度90901.0131.013气相分率00.344摩尔流量 kmol/hr8401.048401.07-530.562-530.544H2O129481129482N28.6778.677SO20.0750.075C

15、O221765.221766.5H+tracetraceOH-0.0810.081HCO3-882.153880.423SO2trace0.075CO290.69921765.2H+tracetraceOH-0.0290.081HCO3-30933882.153NH3447.0048929.5NH4+11200.82216.55HSO3-33.041485.629SO32-4547.624100.56表 4-8 V0201 闪蒸罐前后物流结果表项目进料流股出料流股出料流股温度9090901.0131.0131.013气相分率0.34401摩尔流量kmol/hr8401.075513.15288

16、7.93质量流量kg/hr64425.4体积流量cum/hr85654.3104.18685550.4-530.544-368.957-161.586组分流量kg/hrH2O1294829470634775.9N28.6770.0018.677SO20.0750.0010.075CO221766.58.85221757.7H+tracetrace0.00OH-0.0810.0810.00HCO3-880.423880.3110.00NH38930.071047.097883.05NH4+2215.952215.870.00HSO3-486.018486.2050.00SO32-4100.174

17、099.990.00NH38929.58930.07NH4+2216.552215.95HSO3-485.629486.018SO32-4100.564100.17表 4-9 E0202 换热器前后物流结果表表 4-10 E0203 换热器前后物流结果表项目进料流股出料流股温度90201.0131气相分率10.014摩尔流量 kmol/hr2887.932426.33项目进料流股出料流股温度-49.92011气相分率10.99摩尔流量 kmol/hr26521.726413.5790517790517490816636883-384.309-374.973H2O11229.39279.36N2

18、620280620280SO20.001traceCO2155030150266H+0.00traceOH-0.000.001HCO3-0.006604.35NH33977.742134.41NH4+0.001952.37HSO3-0.00traceSO32-0.000.001表 4-11 E0204 换热器前后物流结果表项目进料流股出料流股温度19.4-4011气相分率0.910.887摩尔流量 kmol/hr28805.928713.2854942854942636892492745-569.285-591.124H2O3512933458.864425.464425.485550.486

19、2.555-161.586-194.312H2O34775.926460.1N28.6778.677SO20.075traceCO221757.71443.15H+0.00traceOH-0.000.002HCO3-0.0028165.3NH37883.0521.845NH4+0.008326.21HSO3-0.000.001SO32-0.000.093表 4-12 V0202A 闪蒸罐前后物流结果项目进料流股出料流股出料流股温度-40-40-40111气相分率0.88710摩尔流量kmol/hr28713.225469.13244.14质量流量kg/hr85494276653388409体积

20、流量cum/hr49274549267866.908-591.124-324.611-266.513组分流量kg/hrH2O33458.8109.39533349.4N26202896202862.644SO2tracetracetraceCO21461371461370.092H+trace0.00traceN2620289620289SO2tracetraceCO2150218146137H+tracetraceOH-0.013traceHCO3-36837.542494.5NH31579.080.165NH4+10889.912562.2HSO3-0.0010.001SO32-0.094

21、0.094表 4-13 E0205 换热器前后物流结果表项目进料流股出料流股温度-40011气相分率00.001摩尔流量 kmol/hr3244.143244.41884098840966.90871.872-266.513-264.556H2O33349.433354.3N22.6442.644SO2tracetraceCO20.09212.225H+tracetraceOH-trace0.001HCO3-42494.542477.7NH30.1014.796NH4+12562.212557.2HSO3-0.0010.001OH-trace0.00traceHCO3-42494.50.004

22、2494.5NH30.1650.0640.101NH4+12562.20.0012562.2HSO3-0.0010.000.001SO32-0.0940.000.094表 4-14 V0202B 闪蒸罐前后物流结果表项目进料流股出料流股出料流股温度000111气相分率0.00110摩尔流量kmol/hr3244.410.233244.18质量流量kg/hr884098.78288400.2体积流量cum/hr71.8725.19766.675-264.556-0.014-264.542组分流量kg/hrH2O33354.30.02533354.3N22.6442.2620.381SO2trac

23、etracetraceCO212.2256.4945.73H+trace0.00traceOH-0.0010.000.001HCO3-42477.70.0042477.7NH34.7960.0014.796NH4+12557.20.0012557.2HSO3-0.0010.000.001SO32-0.0930.000.093SO32-0.0940.093表 4-15 M0201 结晶器前后物流结果表表 4-16 S0201 分离器前后物流结果表项目进料流股出料流股出料流股温度000111固相分率0.2501项目进料流股出料流股温度0011气相分率00摩尔流量 kmol/hr3244.18259

24、5.9288400.288400.266.67567.791-264.542-268H2O33354.333358.1N20.3810.381SO2tracetraceCO25.7315.119H+tracetraceOH-0.0010.001HCO3-42477.72896.05NH34.7968.429NH4+12557.2856.166HSO3-0.0010.002SO32-0.0930.092NH4HCO30.0051265.9表 4-17 碳铵冷却结晶工段总物料衡算项目进料流股出料流股流股信息脱硫烟气氨法脱硫残余液亚硫酸铵溶液副副-碳废气-N2+CO2铵温度-49.945.690-4

25、00011.0131.013111气相分率100101固相分率000010摩尔流量kmol/hr26521.77908.555513.1525469.1648.4781947.44摩尔流量kmol/hr2595.921947.44648.478质量流量kg/hr88400.237134.451265.9体积流量cum/hr67.79110.31532.324-268-136.728-131.738组分流量kg/hrH2O33358.133358.10.001N20.3810.381traceSO2tracetracetraceCO215.11915.111traceH+tracetracetr

26、aceOH-0.0010.001traceHCO3-2896.052898.06traceNH38.4298.426traceNH4+856.166856.17traceHSO3-0.0020.002traceSO32-0.0920.092traceNH4HCO351265.90.0051265.94.4 牛磺酸工段图 4-3 牛磺酸工艺示意图质量流量kg/hr79051776653351265.937134.4体积流量cum/hr490816148.843104.32410.315-384.309-567.168-368.957-324.611-131.738-136.728组分流量kg/h

27、rH2O11229.312060994706109.3950.00133358.1N26202808.6770.001620286trace0.381SO20.001trace0.001tracetracetraceCO215503090.6998.852146137trace15.111H+0.00tracetrace0.00tracetraceOH-0.000.0290.0810.00trace0.001HCO3-0.0030933880.3110.00trace2898.06NH33977.74447.0041047.090.064trace8.426NH4+0.0011200.8221

28、5.870.00trace856.17HSO3-0.0033.041486.2050.00trace0.002SO32-0.004547.624099.990.00trace0.092NH4HCO3-51265.9-由工艺示意图可知，牛磺酸工段包括反应器、换热器、闪蒸罐和结晶器等重要单元过程，需要对它们进行物料衡算。表 4-18 E0302 换热器前后物流结果表表 4-19 E0301 换热器前后物流结果表项目进料流股出料流股温度90.115055气相分率00.234摩尔流量 kmol/hr5513.155527.67103444103444104.1748979.65-368.945-349

29、.897H2O9470694967.8N20.0010.001SO20.0019.616CO28.879641.621H+trace0.001项目进料流股出料流股温度122.515055气相分率11摩尔流量 kmol/hr84843700.473700.47530.828571.852-0.956-0.919C2H4O3700.473700.47表 4-20 R0301 牛磺酸反应器前后物流结果表项目进料流股进料流股出料流股温度5气相分率0.23410.243摩尔流量kmol/hr5527.67845568.95质量流量kg/hr1034443700.47107145体积流量cum/hr897

30、9.65571.8529638.59-349.897-0.919-341.778组分流量kg/hrH2O94967.80.0095741.8N20.0010.000.001SO29.6160.0014.794CO2641.6210.00643.461H+0.0010.000.001OH-0.020.000.003HCO3-3.0040.000.452NH32130.470.001438.8NH4+1068.410.001028.15OH-0.0810.02HCO3-880.2723.004NH31047.492130.47NH4+2215.451068.41HSO3-488.0784453.2

31、8SO32-4098.14170.186表 4-21 E0303 换热器前后物流结果表表 4-22 E0304 换热器前后物流情况表项目进料流股出料流股温度1509055气相分率0.2680摩尔流量 kmol/hr5575.715561.3410793810793810348.4111.037-353.035-372.755项目进料流股出料流股温度123.315050.5气相分率11摩尔流量 kmol/hr1818792.957792.957114.0151262.53-0.205-0.196C2H4O792.957792.957HSO3-4453.280.001144.06SO32-170.

32、1860.001.416C2H4O0.003700.471813.01C2H6NO3S0.000.005318.83表 4-23 V0301 闪蒸罐前后物流情况表项目进料流股出料流股出料流股温度9090900.40.40.4气相分率010摩尔流量 kmol/hr5561.345301.52277.2921079389720910728.8111.0563989809.795-372.764-298.469-22.209H2O95677929473044.82N20.0010.001traceSO20.001198.2450.005H2O95935.995677N20.0010.001SO21.

33、0690.001CO2642.64311.017H+0.001traceOH-0.0010.072HCO3-1.586877.309NH31246.77954.998NH4+10331342.03HSO3-266.20343.789SO32-4.239225.226C2H4O2121.072121.07C2H6NO3S6685.256685.25表 4-24 E0305 换热器前后物流情况表项目进料流股出料流股温度90411气相分率00摩尔流量 kmol/hr277.292277.29210728.810728.89.7959.451-22.209-22.622H2O3044.823044.8

34、2N20.000.00SO20.0050.001CO20.0030.001H+0.0010.001OH-tracetraceCO211643.7830.003H+trace0.000.001OH-0.0720.00traceHCO3-877.3320.000.001NH3954.9731300.010.338NH4+1342.060.00976.257HSO3-43.7010.0020.016SO32-225.3130.000.939C2H4O2121.072119.921.153C2H6NO3S6685.250.006685.25表 4-25 M0301 结晶器前后物流情况表项目进料流股出料

35、流股温度3.32011气相分率00固相分率00.14摩尔流量 kmol/hr437.261383.40415372.615372.611.2518.02-33.958-30.286H2O3770.073769.98N20.000.00SO216.49116.174CO20.0040.004H+80.326.05OH-tracetraceHCO3-tracetraceNH3tracetraceHCO3-0.0010.005NH30.3380.001NH4+976.257976.614HSO3-20.01718.424SO32-0.9382.516C2H4O1.1531.153C2H6NO3S66

36、85.256685.25表 4-26 S0301 固液分离器前后物流情况表项目进料流股出料流股出料流股温度202020111气相分率000固相分率0.1410摩尔流量kmol/hr383.40453.852329.552质量流量kg/hr15372.66739.538633.07体积流量cum/hr8.022.15.919-30.286-5.617-24.669组分流量kg/hrH2O3769.98trace3769.98N20.000.000.00SO216.174trace16.174CO20.004trace0.004H+26.05trace26.05OH-tracetracetrace

37、HCO3-tracetracetraceNH4+976.615976.615HSO3-0.1050.506SO32-tracetraceSO42-3842.593842.59C2H4O1.1531.153C2H6NO3S6685.250.00C2H7NO3S0.006739.53表 4-27 牛磺酸工段总物料衡算项目进料流股出料流股流股信息环氧乙烷 1环氧乙烷 2亚硫酸铵溶液硫酸-牛磺酸牛磺酸废气残余液温度122.5123.390.1102020905551110.4气相分率1100001固相分率0000100摩尔流量kmol/hr84185513.1516053.852329.5525301

38、.52质量流量kg/hr3700.47792.957103444156806739.538633.0797209体积流量cum/hr530.82114.01104.174-2.15.91939898085-298.4-0.956-0.205-368.945-5.617-24.66969组分流量kg/hrH2O-94706720trace3769.9892947N2-0.001-0.000.000.001SO2-0.001-trace16.174198.245CO2-8.879-trace0.004643.783NH3tracetracetraceNH4+976.615trace976.615H

39、SO3-0.506trace0.506SO32-tracetracetraceSO42-3842.59trace3842.59C2H4O1.153trace1.153C2H7NO3S6739.536739.530.00C2H6NO3S0.000.000.00图 4-4 硫酸铵精制工艺示意图由工艺示意图可知，硫酸铵精制工段包括换热器、闪蒸罐和结晶器等重要单元过程，需要对他们进行物料衡算。表 4-28 E0401 换热器前后物流情况表项目进料流股出料流股温度2087.60.30.3H+-trace80trace26.050.00OH-0.081-tracetrace0.00HCO3-880.272

40、-tracetrace0.00NH3-1047.49-tracetrace1300.01NH4+-2215.45-trace976.6150.00HSO3-488.078-trace0.5060.00SO32-4098.14-tracetrace0.00SO42-3840trace3842.592119.92C2H4O3700.47792.957-trace1.1530.00C2H7NO3S-6739.530.00-C2H6NO3S-0.000.00-4.5 硫酸铵精制工段表 4-29 V0401 闪蒸罐前后物流情况表项目进料流股出料流股出料流股温度87.61101100.30.30.3气相分率00.316固相分率00摩尔流量 kmol/hr329.552329.5528633.078633.075.91910376.1-24.669-23.394H2O3769.983770.09N20.000.00SO226.0516.574CO20.0040.004H+26.0526.044OH-tracetraceHCO3-tracetraceNH3trace0.001NH4+976.615976.615HSO3-0.5060.001SO32-tracetraceSO42-3842.593842.59C2H4O1.1531.153C2H6NO