学号：201007010122HEBEI UNITED UNIVERSITY 毕业设计说明书中英文摘要G RADUATE D ESIGN A BSTRACT设计题目：年产110万吨焦化厂硫铵工段设设计学生姓名：张忆一专业班级：10化工1班学院：化学工程学院指导教师：高筠教授2014年6月6日摘要本设计为焦油加工厂硫铵工段的工艺设计。

首先，设计中简要的介绍了我国煤化工发展现状及前景，之后阐述了荒煤气中氨回收的作用和意义，本设计还讲到了我国现阶段钢铁企业回收氨的现状。

之后介绍了焦化厂氨回收工艺和当前氨回收技术状况。

之后着重介绍了硫酸铵生产的方法，生产硫铵的方法及途径很多，除了焦化厂中回收氨硫铵工艺，还有如以合成氨为原料生产硫酸铵的工艺等等。

另外，最新开发的硫铵生产工艺为硫铵提供了新的来源，将副产的亚硫酸铵产品用过量的硫酸分解，吸吸再用气氨中和过量的硫酸，制得合格的液体硫酸铵。

液体硫酸铵经浓缩、冷却结晶分离，即可得到固体硫酸铵。

在工艺流程选择中，首先介绍了硫铵的性质及用途，然后从化学原理及硫胺生成的结晶原理两方面介绍了硫酸铵生产工艺原理。

之后讲了硫酸铵结晶的影响因素及控制，优质硫酸铵要求结晶颗粒大，色泽好，强度高，这主要起决于硫酸铵在母液中成长的速率及形成的结晶形壮，对硫酸铵结晶有影响的因素很多，主要有：母液酸度和浓度、母液中的杂质、母液的搅拌等。

接着着重介绍了硫铵生产工艺流程，包括鼓泡式饱和器法制取硫铵，喷淋式饱和器法制取硫铵，酸洗法制取硫铵。

通过各种制取硫铵的工艺的比较，本设计选择了喷淋式饱和器法制取硫铵。

喷淋包和器分为上下两段，上段为吸收室，下段为结晶室。

由上个工段来的煤气进入喷淋包和器的上段，分成两路沿包和器水平方向流动。

每股煤气均经过数个喷头，用含游离酸的母液喷洒，以吸收煤气中的氨。

两股煤气汇合后从切线方向进入饱和器中心旋风分离部分，除去夹带的酸雾滴，从上部中心出口管离开到下一个工段。

饱和器的上段与下段以降液管连通，喷洒吸收氨后的母液从降液管流至结晶室底部，不断搅拌母液，使硫铵晶核长大。

带有小颗粒的母液上升至结晶室上部，大部分至母液循环泵，少部分至母液加热器，用蒸汽加热使母液温度升高。

一方面溶解母液中的小颗粒结晶，减少晶核数量，另一方面保持饱和器内的水平衡（或用煤气预热器维持水平衡），混合后的两部分母液进入大的母液循环泵，送经饱和器的上段进行循环、喷洒。

饱和器的上段设满流管，保持液面并封住煤气，使其不能进入下段，母液在上段与下段之间不断循环，使母液中的晶核不断长大，沉降在结晶室底部，用结晶泵抽至结晶槽，经离心分离，干燥后得成品硫铵。

本设计结合喷淋式饱和器法支取硫酸铵工艺对年产110万吨焦化厂硫铵工段设计。

本设计内容包括:生产原理、工艺流程、计算及设备的选型、工艺布置、操作规程、成本估算等。

本工艺采用主要设备：蒸氨塔，喷淋式饱和器，煤气预热器，沸腾床干燥器等。

首先根据实际的生产要求对氨水蒸馏塔部分进行物料衡算和热量衡算，生产110万吨焦炭所需的干煤量为137.50t ，每小时消耗干煤量156.39t ，剩余氨水量为16391.63kg/h ，可求的剩余氨水的组成，确定剩余氨水含氨量50.0=f x ％。

氨在蒸馏塔中的回收率为98%，分凝器后氨汽操作温度为98℃，操作压力为115kPa ，在此条件下确定氨水分凝器后的成品氨汽组成及含氨浓度%92.11=p x 。

由最小回流比求得实际回流比，在进行塔的物料衡算，得到蒸氨塔的物料平衡图。

接着进行蒸氨塔的热量衡算，输入的热量包括氨水带入的热量、回流液带入的热量、直接蒸汽带入的热量，输出的热量塔顶氨汽带走的热量、废水带走的热量、化学反应吸收的热量。

然后计算蒸馏塔的塔板数，由前计算得的R,x R 等值求出操作线方程，通过逐板计算法计算塔板数为12，塔径为1400mm ，塔高取9.05m 。

然后对氨气分凝器进行物料衡算和热量衡算，求其传热面积78.92m 2，选用 F=81m 2埋入式分凝器1台。

接着对饱和器进行热量衡算和物料衡算。

焦炉煤气量为53954.55Nm 3/h ，首先是氨的平衡，输入的氨量包括焦炉煤气带入量和直接入饱和器的氨汽带入量，输出的热量包括焦炉煤气带出量和生成硫酸铵所消耗的氨量。

硫铵产量为1739.14kg/h ，100％硫酸耗量为1292.05kg/h ，折合成78％的硫酸为1656.47kg/h 。

之后是水平衡，输入的水量包括煤气带入的水量、直接入饱和器的氨汽带入的水量、硫酸带入的水量、离心机洗水量、冲洗饱和器和除酸器带入的水量，输出的水量包括离心机后硫铵带走的水量、煤气应从饱和器的走水。

当母液酸度为6％时，饱和其中母液温度为52℃。

最后通过热量衡算得到煤气经预热后的温度为65.79℃。

饱和器内筒截面积为6.94m 2，内筒直径取3000mm ，外筒直径取4000mm 。

然后是煤气预热器的热量衡算和物料衡算。

热平衡中，输入的热量包括煤气带入的热量和加热蒸汽带入的热量，输出热量包括煤气带出的热量和散热损失。

预热器所需的加热面积为77.06m 2，选用规格为2m 96F =的预热器。

沸腾床硫铵干燥器的热量衡算和物料衡算，计算沸腾床最低流态化速度为0.141m/s,干燥器总截面积为0.342m 2。

干燥器溢流高度是控制沸腾床层高度及物料停留时间的重要参数，基于传热原理，可以通过对固定床高度的计算来确定沸腾床的高度，沸腾床高度（即溢流口高度）取400mm 。

最后是其他设备的选型，离心机选用的卧式单击活塞推料离心机型号为WH-800B 。

结晶槽选用常压碳素钢和低合金钢容器系列中90°无折边锥形底平盖容器系列(JB1423—74系列)，其公称容积 Vn = 8 m³ ，计算容积 V 计 = 7.86 m³。

硫铵高位槽公称容积V N= 25 m3，公称直径D N=2000mm，长度L = 5800mm。

母液循环泵选用耐腐蚀泵，型号为100Fz-40流量100 m3/h.扬程40m。

旋风分离器选用XLP/A—10.6型旋风分离器处理风量11100 m3/h，外形尺寸φ1060× 4545。

本设计还绘制了生产工艺流程图、饱和器装配图、车间平面布置图，并撰写了设计说明书。

关键词: 煤化工；硫铵生产工艺；喷淋式饱和器AbstractThis design for tar processing factory of ammonium sulfate section process design.First of all, the design is briefly introduced in the coal chemical industry development present situation and prospects in our country, then expounds the function and significance of the ammonia in the waste gas recovery, this design also talked about the current situation of China's iron and steel enterprises at present stage recovery of ammonia.After introduced the coking plant of ammonia recovery process and ammonia recovery technology of the current situation.Then emphatically introduces the method of ammonium sulfate production, the production method and way of ammonium sulfate, ammonium in addition to the recovery of ammonia and sulfur in the coking plant technology, and such as taking ammonia as raw material to produce ammonium sulfate process, and so on.In addition, the latest development of ammonium sulfate production technology provides a new source of ammonium sulfate, by-product ammonium sulfite products with excess sulfuric acid decomposition, absorbing excess gas ammonia neutralization of sulfuric acid, ammonium sulfate was qualified liquid.Liquid by cooling crystallization separation, enrichment, ammonium sulfate can be solid ammonium sulfate.In process selection, first introduced the properties and USES of ammonium sulfate, and then from the chemical principle and two aspects of the crystallization of thiamine generating principle of ammonium sulfate production process principle are introduced.After talked about the influence factors and control of ammonium sulfate crystallization, high quality ammonium sulfate requires crystal particles, good color, high strength, the main fact in formation rate and growing up in mother liquor of ammonium sulfate crystal shape and a number of factors which have influence on ammonium sulfate crystallization, mainly include: mother liquor acidity and concentration, the impurity in the mother liquor, mixing of mother liquor etc.Then emphatically introduces the ammonium sulfate production process, including bubbling saturator legal system in ammonium sulfate, spray-type saturator of ammonium sulfate, pickling legal system for ammonium sulfate.Through a variety of preparing ammonium sulfate process of comparison, this design chose the spray-type saturator legal system for ammonium sulfate.Spray package and device is divided into two segments, for absorption in the upper chamber, the room forcrystallization.By the last section of gas into a spray of package and section, all is divided into two bags and horizontal direction.Gas per share have been a number of nozzle, the use of free acid mother liquor spraying, to absorb the gas of ammonia.Two strands of the gas from the tangent direction after convergence part into the heart of the saturator cyclone separation, remove the entrained acid fog drop, away from the upper center outlet pipe to the next section.Saturator in the upper and under paragraphs to downcomer connected, the mother liquor after spraying the absorption of ammonia from downcomer flow to crystal at the bottom of the chamber, stirring constantly mother liquor, the ammonium sulfate crystal nucleus to grow up.With small particles of mother liquid crystal rose to the upper chamber, most to mother liquor circulating pump, a few to mother liquor heaters, mother liquor with steam heating temperature.On the one hand, dissolve the small particles crystallization mother liquor, reduce the number of crystal nucleus, on the other hand, keep the balance of the water in the saturator (or use the gas heater to maintain water balance), after mixing the two parts of mother liquor into the big mother liquid circulating pump, let off period on circulation, spraying saturator.The saturator in full flow tube, maintain the liquid level and sealed gas, make its can't into the next section, mother liquor in the cycle between and under paragraphs, make the crystal nucleus of mother liquor grown, settlement in crystal at the bottom of the chamber, with crystal pumped to the crystallizer, the centrifugal separation, drying after finished product ammonium sulfate.This design combines spray-type saturator method of withdrawal, ammonium sulfate process of annual output of 1.1 million tons of coking plant ammonium sulfate section design.This design content includes: the production principle, process flow, calculation and equipment selection, process layout, operation procedure, cost estimation, etc.This process is the main equipment: steamed ammonia tower, spray-type saturator, gas preheater, bullate bed dryer, etc.First according to the requirements of the actual production of ammonia distillation tower parts for material balance and heat balance, dry coal quantity required for the production of 1.1 million tons of coke is 137.50 t, 156.39 t dry coal consumption per hour, the amount of residual ammonia is 16391.63 kg/h, ask for the composition of residual ammonia, determine the residual ammonia ammonia content %.Ammonia recovery rate of 98%, in the distillation tower dephlegmator ammonia vapor after the operating temperature is 98 ℃, the operating pressure of 115kpa, in this condition to determine ammonia condenser after the finished product of ammonia stripper and ammonia concentration.The actual reflux ratio obtained by minimum reflux ratio and tower of material balance, get steamed ammonia mass balance of the tower.Then steamed ammonia tower heat balance, heat input, including ammonia into heat, backflow into the quantity of heat, steam directly into heat and the heat output of ammonia stripper tower top take away heat, the waste water quantity of heat, chemical reaction heat absorption.Then calculate distillation column plate number, by the former calculation of R,x and operating line equation, theRequivalent plate number by plate count method calculation of 12, the tower diameter is 1400 mm, height of 9.05 m.And then to the ammonia condenser for material balance and heat balance, its heat transfer area of 78.92 m2, choose F = 81 m2 embedded dephlegmator 1.Then the saturator heat balance and material balance.Amount of coke oven gas is 53954.55 Nm3/ h, the first is the balance of ammonia, the input amount of ammonia, including coke oven gas into the quantity and amount of ammonia vapor into directly into the saturator, heat output, including coke oven gas out of the amount of ammonia consumption amount and generate ammonium sulfate.ammonium sulfate production of 1739.14 kg/h, 100% sulfuric acid consumption is 1292.05 kg/h, converted into 78% of sulfuric acid is 1656.47 kg/h.Followed by water balance, the input of water gas is included into the water, directly into the saturator of ammonia gas into water, acid into water, centrifuge washing water, washing saturator, and in addition to the acid into the water and the output of ammonium sulfate away after water including centrifuge, the amount of water and gas from saturator slice.When the mother liquor acidity is 6%, saturated with mother liquor for 52 ℃ temperature.The gas is obtained by heat balance after preheating temperature of 65.79 ℃.Within the saturator tube cross-sectional area is 6.94 m2, inner tube diameter is 3000 mm, outer tube diameter 4000 mm.And then the gas preheater heat balance and material balance.In thermal equilibrium, heat input, including gas into heat and heat steam into heat, heat output, including the gas out of the heat and heat loss.Preheater the heating area of 77.06 m2, with specifications for the preheater.Sulfur ammonium bullate bed dryer heat balance and material balance, calculate the bullate bed minimum fluidization velocity of 0.141 m/s, dryer a total area of 0.342 m2.Dryer overflow height is to control the bullate bed layer height and stay time of important material parameters, based on the heat transfer principle, the calculation offixed bed height to determine the height of the bullate bed, bullate bed height (i.e., the overflow mouth height) for 400 mm.Finally the other equipment selection, the horizontal centrifuge choose click the pistons pushing centrifuge model for WH - 800 B Crystallizer selects the atmospheric carbon steel and low alloy steel container series 90 ° no ruffled cone bottom flat cover container series (JB1423-74 series), its nominal capacity Vn = 8 m³,calculate the volume V C = 7.86 m³.ammonium sulfate elevated tank nominal volume V = 25 m3, nominal diameter D = 2000 mm, length L = 5800 mm.Mother liquor circulation pump corrosion resistant pump, models for 100 F Z- 40 flow 100 m3 / h head 40 m.Choose XLP/A cyclone separator - 10.6 type cyclone separator of 11100 m3/ h, overall dimensionsϕ45451060⨯.This design also made the production process flow diagram, saturator assembly drawing, workshop layout, and writing the design specification. Keywords: Coal Chemical Industry; ammonium sulfate process; bubble-umbrella-type saturator。