甲醇精馏技术 毕业论文
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甲醇精馏技术
一.内容提要
甲醇最早由木材和木质素干馏制的，所以俗称木醇。
化学分子式CH30H，无色、透明高度挥发、易燃液体。
近年来，世界甲醇的生产能力发挥速度较快。
甲醇工业的迅速发展，是由于甲醇是多种有机产品的基本原料和重要的溶剂，广泛用于有机合成、染料、医药和国防等工业。
由甲醇转化为汽油方法的研究成果，从而开辟了由煤转换为汽车燃料的途径。
甲醇工业已成为化学工业中一个重要的领域。
关键词：甲醇精馏物料衡算
目录
1甲醇精馏工艺简概 (1)
1.1甲醇的性质于用途 (1)
1.1.1甲醇性质 (1)
1.1.2甲醇用途 (1)
1.2甲醇精馏工艺概况 (2)
1.2.1工序任务 (2)
1.2.2装置工艺 (2)
1.2.3工艺参数选择 (2)
2甲醇精馏生产工艺设计与计算 (4)
2.1物料衡算 (4)
2.2回流比确定 (5)
2.3理论塔板数计算 (6)
3 精馏设备图简介 (8)
总结 (12)
参考文献 (13)
致谢.......................................................................错误！未定义书签。
附图纸. (15)
1甲醇精馏工艺简概
1.1甲醇的性质于用途
1.1.1甲醇性质
甲醇又名木醇，是一种最简单的饱和醇。
甲醇是无色有酒精气味易挥发的液体，熔点-93.9°C、沸点64.7°C，能溶于水和许多有机溶剂。
甲醇有毒，大量饮用会导致死亡。
甲醇易燃，其蒸气与空气能形成爆炸混合物，甲醇完全燃烧生成二氧化碳和水蒸气，同时放出热量：2CH3OH+3O2=2CO2+4H2O
甲醇有较强的毒性，对人体的神经系统和血液系统影响最大，它经消化道、呼吸道或者皮肤摄入都会产生毒性反应，甲醇蒸气能损害人的呼吸道粘膜和视力。
甲醇中毒后，通常可以用乙醇解读法。
其原理是因为甲醇本身无毒，而代谢产物有毒，因此可以通过抑制代谢的方法来解毒。
甲醇和乙醇在人体的代谢都是同一种酶，而这种酶和乙醇更具亲和力，甲醇中毒者，可以通过饮用烈性酒（酒精毒通常在60度以上）的方式来缓解甲醇代谢，进而使之排除体外，而甲醇已经代谢产生的甲酸，可以通过服用小苏打（碳酸氢钠）来中和。
1.1.2甲醇用途
随着技术的发展和能源结构的改变，甲醇开辟了许多新的用途。
甲醇用途广泛，是基础的有机化工原料和优质燃料，主要应用于精细化工、塑料等领域，用来制造甲醛、醋酸等多种有机产品，也是农药、医药的重要原料之一。
甲醇在深加工后可作为一种新型清洁燃料，并
且容易输送，可以单独或与汽油混合作为汽车燃料。
甲醇的消费已超过其传统用途，潜在的耗用量远远超过其化工用途，特别是随着能源结构的改变，甲醇有未来主要燃料的候补燃料之称，需用量十分巨大。
1.2甲醇精馏工艺概况
1.2.1工序任务
甲醇精馏是甲醇合成的下游工序，其目的就是对合成装置来的粗甲醇进行精制，将甲醇中的杂质进行脱除，以生产符合标准的优等级精甲醇产品。
1.2.2装置工艺
目前，总体来说甲醇精馏的工艺大体分为两塔工艺流程和三塔工艺流程，根据塔内件的不同可分为塔盘精馏、填料精馏和复合型精馏。
精馏的主要设备是精馏塔，而塔的内件是实现气液接触和热质传递的主要元件，常用的塔内件分塔盘和填料两种。
热量自塔釜输入，物料在塔内经多次部分气化与部分冷凝进行精馏分离，由冷凝器和冷却器中的冷却介质将余热带走。
此过程中，热能利用率很低，为此，在确定流程是应考虑余热的利用，注意节能。
1.2.3工艺参数选择
(1)操作压力的选择
精馏操作可在常压、减压和加压下进行。
压力增加可提高塔的处理能力，但会增加塔身的壁厚，导致设备费用增加；压力增加，组分见的相对挥发度降低，回流比或塔高增加，导致操作费用增加；压力增加，组分间的相对挥发度降低，回流比或塔高增加，导致操作费用
或设备费用增加。
因此如果在常压下操作是，塔顶蒸气可以用普通冷却水进行冷却，一般不采用加压操作。
(2)进料热状况的选择
进料热状态以进料热状况参数q表达。
进料状态有5种，进料为过冷液体：q > 1 ，饱和液体：q=1 ，气、液混合物：0 <q <1 ，饱和蒸气：q=0 ，过热蒸气：q <0 。
对于低温干馏，不论D/F（塔顶出料量/进料量）值如何，采用较高的q值为经济；对于高温精馏，当D/F值大时宜采用较小的q值，当D/F值小时宜采用q值较大的气液混合物。
此处已设为q=1
(3)加热方式
蒸馏一般采用简洁蒸气加热，设置再废器，但对塔底产物基本是水，且在低浓度是的相对挥发度较大的体系，也可采用直接蒸气加热。
但由于直接蒸气的加入，对釜内溶液起到一定稀释作用，在进料条件和产品纯度、轻组分收率一定的前提下，釜液浓度相应降低，故需在提馏段增加塔板以达到生产要求。
(4)回流比的选择
由于回流比的大小不仅影响到所需理论板数，还影响到加热蒸气和冷却水的消耗量，以及塔板、塔径、蒸馏釜和冷凝器的结构尺寸的选择，因此，适宜回流比的选择是一个很重要的问题。
R=1.2Rmin
2甲醇精馏生产工艺设计与计算
2.1物料衡算
精馏装置图2-1
已知：M=30.23kg/kmol M甲醇=32.04kg/kmol M水=18.02kg/kmol 进料流量F=Ws=73734.6kg/h 甲醇的质量分率Wt=87% 水的质量分率Wt=13% 摩尔分率单位：%
Ws=73734.6/30.23=2439.1201kmol/h
进料的摩尔流量 F=
M
甲醇的摩尔分率X f =((87×73734.6/100)/32)/2439.1201=0.82 D=966.2289kmol/h W=1552.1203kmol/h Xw=0.67
根据物料衡算方程 F=D+W
F×X f =D×X D +W×Xw
计算出 2439.1201×0.82=966.2289×X D +1552.1203×0.67 X D
=0.994
进料温度 t F (1000kpa) t F =107.2°C 取泡点进料q=1
塔顶温度为t D =128.1°C
在t F =107.2°C 温度下，根据安托因公式计算出甲醇和水的饱和蒸气
压，注：水的安托因常数为A=7.1827 B=1722.632 C=232.7987 LgP °=A —C
t B + 式中 P °------饱和蒸气压，Kpa t-------物系温度，°C 代入数据中，得水的饱和蒸气压P °B =130.652kpa
甲醇的安托因常熟为A=18.5875 B=3626.55 C=－34.29
LnP °=A —C
T B + 式中 P ° ------饱和蒸气压 ，mmHg T-------物系温度 ，K 代入数据得，甲醇的饱和蒸气压P °A =442.77kpa
2.2回流比确定
由于进料为泡点进料q=1，所以画q 线与平衡线交点，用交点坐标x,y 求最小回流比。
做图法求最小回流比
α=P °A / P °B =442.77/130.652=3.39
Rmin=X D —Yq / Yq —Xq=994—933.5818/933.5818—
820=0.5319
操作回流比可取为最小回流比的 1.1～2.0倍，所以取 R=1.2Rmin=1.2×0.5319=0.6383
所以，回流比确定为R=0.6383
L=R ×D=0.6383×966.2289=617.0337kmol/h
L'=L+q ×F=617.0337+1×2439.1201=3056.1538kmol/h
V'=V=1583.2626kmol/h
2.3理论塔板数计算
精馏段操作线方程为 y=
1+R R x+X D /R+1 截距 ： X D /R+1 =1
6383.0994.0+=0.6067 连接（X D ，X D ），（0，X D /R+1 ）与 q 线交于d 点，连接（Xw, Xw)与d
点，得到提馏段操作线，然后，由平衡线与操作线可得精馏塔理论板数，但由于Xw 极小，利用作图法画出理论板数，如图所示，梯级数为12块。
因为塔底设有再沸器，所以精馏塔理论半数要比梯级数少1，所以精馏塔理论板数为11块，精馏段为10块，提馏段为1块。
3 精馏设备图简介
精馏装置有精馏塔、原料预热器、再沸器、冷凝器、釜液冷却器和产品冷却器等设备。
塔设备的类型根据塔内气液接触部件的结构形式，可分为板式塔和填料塔两大类。
图1—带中间再沸器和中间冷凝器的精馏塔
板式塔是一类用于气液或液液系统的分级接触传质设备，由圆筒形塔体和按一定间距水平装置在塔内的若干塔板组成。
广泛应用于精馏和吸收,有些类型（如筛板塔）也用于萃取，还可作为反应器用于气液相反应过程。
操作时（以气液系统为例），液体在重力作用下,自上而下依次流过各层塔板,至塔底排出；气体在压力差推动下，自下而上依次穿过各层塔板，至塔顶排出。
每块塔板上保持着一定深度的液层，气体通过塔板分散到液层中去，进行相际接触传质。
图2—板式塔的结构
1—塔壳体； 2—塔板； 3—溢流堰；
4—受液盘； 5—降液管
填料塔是一类用于气液和液液系统的微分接触传质设备，主要由圆筒形塔体和堆放在塔内对传质起关键作用的填料等组成，用于吸收、蒸馏和萃取，也可用于接触式换热、增湿、减湿和气液相反应过程。
由塔体、填料、填料的压板和支承板、液体分布器和液体再分布器等组成。
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图3—填料塔的结构示意图
1—塔壳体；2—液体分布器；3—填料压板；4—填料；
5—液体再分布装置；6—填料支撑板
再沸器用以将塔底液体部分汽化后送回精馏塔，使塔内汽液两相间的接触传质得以进行。
小型精馏塔的再沸器，传热面积较小，可直接设在塔的底部，通称蒸馏釜。
大型精馏塔的再沸器，传热面积很大，与塔体分开安装，以热虹吸式和釜式再沸器最为常用。
热虹吸式再沸器是一垂直放置的管壳式换热器。
液体在自下而上通过换热器管程时部分汽化，由在壳程内的载热体供热。
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图4—垂直人热虹吸式再沸器
冷凝器用以将塔顶蒸气冷凝成液体，部分冷凝液作塔顶产品，其余作回流液返回塔顶，使塔内汽液两相间的接触传质得以进行。
最常用的冷凝器是管壳式换热器。
小型精馏塔的冷凝器可安装在精馏塔顶部；大型的冷凝器则单独安装,并设有回流槽,回流液用泵送至塔顶。
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总结
在石油炼制石油化工和其他化工生产中，精馏塔是应用极为广泛的传质过程。
其目的是使混合液中的各组分进行分离，使之达到规定的纯度。
精馏塔过程要消耗能量，根据相关数据表明，在石油化工行业的总能耗中，大约有40％一50％消耗在精馏塔过程。
因此可以说精馏塔装置是耗能最大的单元之一。
此外，精馏塔是一个典型的多输入多输出对象，它的通道很多，动态响应缓慢，内在机理复杂，参数间相互关联，各塔的工艺结构千差万别，且对控制要求不断提高。
因此精馏塔的控制极为重要。
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参考文献
[1]宋维端，甲醇工学，化学工业出版社。
[2]葛婉华，化工计算，化学工业出版社。
[3]汪镇安，化工工艺设计手册，化学工业出版社。
[4]化工原理（上册），姚玉英主编，天津科学技术出版社。
[5]化工原理（下册），姚玉英主编，天津科学技术出版社。
[6]化工原理课程设计，天津大学化工原理教研室编。
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甲醇精馏工艺流程图
甲醇精馏工艺流程图
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15。