河南城建学院本科毕业设计设计说明
设计说明
目前氨合成的方法，由于采的压力、温度和催化剂种类的不同，一般可分为低压法、中压法和高压法三种。目前我国中小型合成氨厂合成操作压力大多为20-35MPa.本设计应该采用中压法，操作压力为32MPa。合成氨的生产方法主要包括三个步骤：一是选气，二是净化，三是压缩和合成。本设计是12万吨每年合成氨合成的工艺计算。合成氨生产所用的催化剂活性温度在400-500℃。一些小型合成氨厂合成压力在30MPa，空间速度选择在2000-3000每小时之间。从氢氮混合气体中分离氨的方法大致有2种：水吸收法和冷凝法。本设计采用冷凝法。一般含氨混合气体的冷凝分离是经水冷却器和氨冷器两步实现的。液氨在氨分离器中与循环气体分开，减压送入贮槽。贮槽压力一般为1.6-1.8MPa，此时，冷凝过程中溶解在液氨中的氢、氮和惰性气体大部分可减压释放出来。
合成塔进口气体组成包括氢氮比、惰性气体含量和塔进口氨含量。本设计中，进塔气体的氢氮比控制在3.074比较适宜。循环气体中惰性气体的控制还与操作压力和催化剂活性有关。操作压力比较高，及催化剂活性比较好时，惰性气体的含量可以高一些。本设计中惰性气体的体积分数为15%。进口氨含量还与合成操作压力和冷凝温度有关。压力高，氨合成反应速度快，进口氨含量可适当控制高一些。压力低，为保持一定的反应速度，进口氨含量可适当控制低一些。本设计中氨的进口含量为2.5%。
本设计工艺计算总结：催化剂筐内径φ422。合成塔催化剂总高6.550m。其中绝热层高0.78m。采用φ500扁平管。催化剂总装填量为0.714m。进塔气量175518m3/h。
关键字：合成氨，中压法，空间速度，催化剂
Design Notes
Design Notes
The current method of ammonia synthesis, due to adopt the pressure, temperature and catalyst species, generally can be divided into low pressure, medium pressure and high pressure method three. Synthesis of small and medium sized ammonia plant is currently operating pressure of mostly 20-35MPa. The design should be ud in the pressure method, the operating pressure of32MPa. Ammonia production methods consists of three steps: First, choo gas, and cond, purification, compression and synthesis of third. This design is 12 tons per year of synthetic ammonia synthesis process calculation. The catalyst ud in ammonia production activity of temperature 400-500 ℃. Synthetic ammonia plant some small pressure 30MPa, hourly space velocity chon between 2000-3000. From the paration of hydrogen and nitrogen mixed gas of ammonia generally have two kinds of methods: water absorption and condensation method. The design us a condensation met
hod. General ammonia gas mixture paration by condensing ammonia cooler water cooler and two-step implementation. Ammonia in the ammonia parator and recycling the gas to parate decompression into the tank. Tank pressure is generally 1.6-1.8MPa, this time, the process of condensation of hydrogen dissolved in liquid ammonia, nitrogen and inert gas most of the available vacuum relead.
Reactor consists of imported gas nitrogen ratio of hydrogen, inert gas and the tower, ammonia imports. In this design, nitrogen and hydrogen gas into the tower at 3.074 is more appropriate than the control. Loop control of the gas in the inert gas and operating pressure and the catalyst is also related to the activity. Operating pressure is relatively high, and the catalytic activity is better, the inert gas content can be higher. In this design, the volume fraction of inert gas is 15%. Also with the synthesis of ammonia imports operating pressure and condensing temperature. High pressure ammonia synthesis reaction speed, may be appropriate to control the ammonia content of imports higher. Pressure is low, in order to maintain a certain speed of respon may be appropriate to control the ammonia content of imports lower. Summary of the calculation of the design process: the catalyst basket inner diameter of φ422. The total reactor catalyst high 6.550m. Which insulation storey 0.78m. By φ500 flat tube. The total loading capacity of the catalyst 0.714m. Tap into the gas175518m3 / h.
Keywords: ammonia in the space velocity-pressure condensation catalyst
目录
设计说明........................................................................................................................................... I 设计符号说明.. (iiii)
引言 .............................................................................................................................................. １第一章总论 (2)
1.1 氨的性质 (2)
1.1.1 氨的物理性质 (2)
1.1.2 氨的化学性质 (2)
1.3 文献综述 (3)
1.3.1 合成氨工业的发展 (3)
1.3.2 合成氨工业的现状 (4)
1.3.3 合成氨工业的发展趋势 (4)
第二章流程方案的确定 (6)
2.1生产原理 (6)
英语作文 求职信2.2 各生产方法及特点 (6)
2.3 工艺流程的选择 (7)
2.4 合成塔进口气的组成 (9)
第三章物料衡算 (11)
boiling3.1 计算依据： (11)
3.2 计算物料点流程 (11)
3.3 物料计算 (12)
3.3.1 合成塔入口气组分 (12)
3.3.2 合成塔出口气组分 (12)
3.3.3 合成率： (13)
3.3.4 氨分离器气液平衡计算 (14)
3.3.5 冷交换器气液平衡计算 (17)
information
3.3.6 液氨储槽气液平衡计算 (18)
3.3.7 液氨储槽物料计算 (21)gon
3.3.8 合成塔物料计算 (24)
3.3.9 水冷器物料计算 (24)
3.3.10 氨分离器物料计算 (25)
3.3.11 冷交换器物料计算 (25)
3.3.12氨冷器物料计算 (26)
3.3.13 氨贮槽物料计算 (30)
第四章热量衡算 (31)
4.1 冷交换器热量计算 (31)
4.2氨冷器热量计算 (33)
pro face4.3循环机热量计算 (35)
4.4合成塔热量计算 (37)
4.5废热锅炉热量计算 (39)
4.6热交换器热量计算 (40)
18hour4.7水冷器热量计算 (42)
4.8氨分离器热核算 (44)
第五章氨合成塔催化剂层设计 (46)
5.1基本数据计算 (46)
5.2分段计算 (47)
5.3反算设计参数的合理性 (52)
设计结果 (54)
参考文献 (55)
附录 (56)
致谢 (57)
设计符号说明
符号名称单位
N NH3合成塔中生成氨的气体摩尔流量kmol / h
N0出合成塔气体摩尔流量kmol / h
y NH3 O 出合成塔气体中氨含量 %
y NH3 I 进合成塔气体中氨含量 %
Δy NH3氨净值 %
V补新鲜补充气体量3m (标) V放放空气量3m (标) V弛弛放气量3m (标) y8i出合成塔某气体组分的含量 %
L19i液氨储槽出口某组分液体量3m (标) V20i液氨储槽出口某组分弛放气量3m (标) L21i液氨储槽入口液体某组分量 %
永远的英文
V5i入合成塔某组分气量3m (标)
V8i 出合成塔某组分气量3m (标)
早教英文儿歌
V10入水冷器进器物料量3m (标)
V11入出水冷器某组分气体量3m (标)
y1i氨冷器进器某组分气体百分含量 %
V2i氨冷器出口某组分气量3m (标)
y2i氨冷器出口某组分气体百分含量3m (标)
C p 比热容kJ /(kmol℃) . P c 临界压力MPa
T C 临界温度℃
P r 对比压力
T r 对比温度
Z压缩因子
淘汰的英文λ导热系数kJ / (m.h. ℃) α给热系数kJ / (m.h. ℃) W 重量流量kg / h
R e 雷诺准数
F 换热面积m2
ρ气体密度kg/ 3m
relaxing是什么意思
Δt m 平均传热温差℃
