设计与计算
[收稿日期]2000-11-20 修回日期:2001-02-23
[作者简介]张丽华(1956-)，女，辽宁大连人,1986年毕业于
青海大学化工工艺专业，工程师，现从事工艺设计工作。
张丽华，刘桂香
(中石化南化公司连云港碱厂，江苏连云港 222042)
[摘要] 为满足生产规模扩大的需要，新增设了淡液蒸馏系统气体冷却器，并对其工艺流程作了简要说明。介绍了该系统热量衡算方法及计算结果。 [关键词] 淡液蒸馏系统；热量计算全部视频列播放表本站
[中图分类号]T Q 015.2 [文献标识码]A [文章编号]1006-7906(2001)03-0043-02
1 引 言
我厂原淡液蒸馏未设独立的气体冷却系统，而是将该气体引入母液蒸馏系统的6台螺旋板换热器进行冷却。随着产量的增加和生产规模的扩大，蒸馏冷凝液(淡液)量比原规模增加。当气温升高时冷却效果不好，氨气温度居高不下，使得吸氨过程的热负荷加大，影响盐水吸氨过程的进行。为此新增了独立的淡液蒸馏冷却系统。2 淡液蒸馏气体冷却系统工艺流程
新增淡液蒸馏系统出气冷却器流程如图1左半部分所示(右半部为母液蒸馏系统出气冷却器)。
超声波放大器图1 蒸馏系统冷器流程
淡液主要来自蒸馏冷却器的含游离氨10mol/L 、二氧化碳3mol/L 的冷凝液，经淡液蒸馏塔加热
蒸馏后，含氨及二氧化碳出气从冷却器的底部进入，与从顶部进入冷却器的冷却水逆流间接换热，将出气温度由85 降至63 ，冷却水温度从32 升至65 。冷却水进水量由冷却器出气温度自调控制。冷却水采用脱盐水，为保证锅炉进水量，由冷却器进水总管的压力调节冷却器进水管与冷却器出水管联通管的流量。淡液蒸馏气体冷却器使用新型波纹管换热器，气体走管程，冷却水走壳程。气体冷凝液沿管壁流下，与从底部进入的热气体逆向流动。这样使得出来的气体冷凝液温度较高，较高的冷凝液温度可降低冷凝液中NH 3和CO 2含量，有利于NH 3和CO 2蒸出与回收，并使冷却气体中NH 3和CO 2含量高。
3 淡液蒸馏气体冷却的目的及控制范围[1]
(1)淡液蒸馏塔出气为水蒸气饱和气体，通过冷却可使气体中大量水分冷凝，气体中NH 3及CO 2得到浓缩。气体在进水吸收系统之前带入的水分减少，可确保吸收系统内盐水的浓度在控制范围内，使吸氨过程顺利进行，减轻吸收系统的负荷。
(2)若气体的温度过低，则靠近混合气体的升华区，一旦进入升华区，即有铵盐析出，堵塞管道。当压力在0kPa(表压)上下时，出气温度一般维持在60~65 为宜。
4 淡液系统气体冷却器设计依据
[2~3]
本设计计算需要的物料数据见表1。
43 2001年第22卷第3期化学工业与工程技术
表1 物料数据
类 别压力
/M Pa 温度
/
组成/mol L-1
NH3CO2
淡液蒸馏塔进液成分 5.35 1.75淡液蒸馏塔出气0.1185
冷却器出气0.10563
冷凝液成分65103
水饱和蒸气压0.0685
水饱和蒸气压0.02463
淡液塔损失量0.050.05 注:(1)淡液蒸馏塔进液流量80m3/h;(2)冷凝液密度1100kg/ m3;(3)冷凝液流量12m3/h。
4.1 淡液蒸馏塔出气流量m1
淡液塔出气中氨气流量:
m1NH
3
=(5.35-0.05) 80=424kmo l/h=7208kg/h
淡液塔出气中二氧化碳气流量:
m1CO
2
=(1.75-0.05) 80=136kmol/h=5984kg/h
淡液塔出气中水蒸气流量:
m1(H
2O)g
=
(m1NH
3
+m1CO
2
)P1H
2
O
(P1总-P1H
2
O
)
=(424+136) 0.59
(1.074-0.59)
=682.6kmol/h=12287kg/h
四合扣4.2 冷却器冷凝液流量m2
冷凝液流量12m3/h由现场分析冷凝液(NH3: 10mol/L、CO2:3mol/L):
m2NH
3
=12 10=120kmol/h=2040kg/h m2CO
2
=12 3=36kmol/h=1584kg/h
4.3 冷却器出气流量m3
冷却器出气流量m3NH
3=m1NH
3
-金属精密成型技术
m2NH
延时冲水阀3
=424
-120=304kmol/h=5168kg/h
冷却器出气流量m3CO
2=m1CO
2
-m2CO
2
=136
-36=100kmol/h=4400kg/h
冷却器出气流量m3(H
2
O)g=
(m3NH
3+m3CO
2
) P3分压
(P3总-P3分压)=
404 0.234 (1.033-0.234)
=118.2kmol/h=2128kg/h
5 淡液蒸馏系统气体冷却器热量衡算[2~4] 5.1 输入热量
5.1.1 冷却器进气带入热量Q1
Q1=m1C p1T1
q1NH
3
=7208 2.219 85=1359537kJ/h
q1CO
2
=5984 0.9211 85=468508kJ/h
q1H
2O
=12287 2651=32572837kJ/h
Q=q1N H
3+q1CO
2
+q1H
2
O
=1359537+468508+32572837=34400882kJ/h 5.1.2 反应热Q2 (1)氨的溶解热q NH
3
溶
:
NH3(g)+H2O(1)=(NH)4OH(aq)-34792kJ/kmol
q NH
3
溶
=120kmol/h 34792kJ/kmol=4175040kJ/h
(2)二氧化碳溶解及中和热q CO
2
:
CO2(g)+H2O(1)+2NH3(aq)=(NH4)2CO3(aq)
-94165kJ/kmol
q CO
2
溶=36 94165=3389940kJ/h
反应热=Q2=q NH
3
溶+q CO2溶=4175040+3389940
=7564980kJ/h
总收入热量=进气热量+反应热
=34758088+7564980=42323068kJ/h
5.2 支出热量
5.2.1 冷却器出气带出热量Q3
Q3=m3c p3T3
Q NH
3
=5168 2.1771 63=708830kJ/h
Q CO
2
=4400 0.9211 63=255329kJ/h
Q H
2
O
=2128 2611.8=5557910kJ/h
Q3=708830+255329+5557910=6522069kJ/h
5.2.2 冷凝液带走热量Q4
Q4=m4c p4T4
=12 1100 3.7681 65=3233029.8kJ/h
5.2.3 冷却水带走热量Q5
总收入热量=总支出热量(热损失忽略不计)，则:
Q5=Q1+Q2-Q3-Q4
=34400882+7564980-6522069-3233030
=3.22 107kJ/h
5.3 冷却水耗量m H
2
O
m H
2
O
=
Q5
S H
2
O
t
=32200000
1000 4.184 33
=233t/h 5.4 换热器面积A
t m=(85-65)-(63-32)
ln
85-65
63-32
冷却塔减震器=25
根据实际使用波纹管冷却器经验,K=580~ 841W/m2 K，则:
A=
Q
K t m
=
32200000
580 3.6 25
=617m2
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