饱和器法生产硫酸铵回收氨

乌海职业技术学院毕业设计

摘 要

煤化工利用生产技术中，炼焦是应用最早的工艺，并且至今仍然是煤化工工业的重要组成部分。炼焦主要产品是生产炼铁用焦炭，同时生产焦炉煤气、苯、萘、蒽、沥青以及碳素材料等产品。

在炼焦过程中，煤中的氮有1.2%~1.5%与芳香烃发生化合反应生产吡啶盐基。其生成量主要取决于煤中氮含量及炼焦温度。一般在煤气初冷器后煤气含吡啶盐基约为0.4~0.6 g/m3，其中轻吡啶盐基约占75%~85%。回炉煤气中吡啶盐基含量约0.02~0.05 g/m3，即回收率达90%~95%。

本设计分别采用饱和器法生产硫酸铵回收氨，中和器法提取粗轻吡啶。对于饱和器法生产硫酸铵的工艺，煤气经鼓风机和电捕焦油器之后进入预热器，然后进入饱和器。煤气穿过饱和器在除酸器分离出液滴后，去脱硫或粗苯回收段。结晶母液用泵从饱和器底部送至结晶槽，沉淀出结晶后满流母液回到饱和器。结晶经分离器，干燥器成为硫酸铵成品。对于中和器法提取粗轻吡啶，母液从结晶槽回流入沉淀槽，同蒸氨分凝器来的氨气一起进入中和器。分解出的吡啶蒸汽等进入冷却器，经油水分离器后上层粗吡啶进入计量槽，放入储槽。下层的分离水返回中和器。

硫酸铵产量1362.6kg/h；硫酸消耗量1367.1kg/h；氨损失率0.54%；带入饱和器总水量1408kg/h；饱和器出口煤气中水蒸气分压7.75kPa；母液最低温度54℃；煤气预热温度 69.6℃；饱和器中央煤气管直径1530 mm；煤气进口管直径1090 mm；饱和器直径5000mm；饱和器高度7740 mm；除酸器进口管外径1660 mm；除酸器直径2720 mm；除酸器出口管在器内部分高度4150 mm；干燥器的沸腾床面积0.778㎡；干燥器直径1000 mm；干燥器溢流口高度388 mm；从反应器回收的吡啶盐基量18.355kg/h；母液处理量1087.29l/h；氨气的分配给中和器的质量分数95.7%；中和器直径1220 mm；中和器筒体高度1220 mm；中和器总高1775 mm；保温面积7.97㎡；设备质量756.03kg

关键词：氮；氨；硫酸；饱和器；母液；硫酸铵：结晶：中和器；粗轻吡啶

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乌海职业技术学院毕业设计

Abstract

Use of coal chemical production technology, the coking process is applied first, and the coal chemical industry is still an important part. Coking main product is the production of iron using coke, while production of coke oven gas, benzene, naphthalene, anthracene, carbon materials, asphalt and other products.

In the coking process, coal nitrogen with 1.2% to 1.5% of ammonia production

with the aromatic pyridine base. Its amount depends on the nitrogen content of coal and coke temperature. Usually early in the gas after the gas cooler containing pyridine base is about 0.4 ~ 0.6 g/m3, which accounts for about 75% light pyridinium ~ 85%. Recycled content of gas in the pyridine base is about 0.02 ~ 0.05 g/m3, the recovery rate of 90% to 95%.

The design of devices were used to the production of ammonium sulfate

saturation recovery of ammonia, medium and light crude pyridine extraction device. Saturated ammonium sulfate for the production of process devices, gas and electricity by the blower after the tar into the preheater, then into the saturator. Saturated gas through the separation device in addition to the acid droplet, the last section of desulfurization or benzene recovery. Crystal liquor pump from the bottom of saturated sent to the crystallizer to precipitate out a full stream after crystallization mother liquor back to saturator. Crystallization by the separators, dryers as ammonium sulfate product. And devices for the extraction of light crude pyridine, mother liquor from the crystallization tank back into the settling tank, with the ammonia to the ammonia segregation device and went into the device. Decomposition of pyridine vapor from entering the cooler through the upper crude oil and water separator after the pyridine into the metering tank, into the tank. Lower returns in the separation of water and the device.

Ammonium sulfate production 1362.6kg / h; sulfuric acid consumption 1367.1kg

/ h; ammonia loss rate of 0.54%; the total amount of water into the saturator 1408kg / h; saturated outlet gas in the steam pressure 7.75kPa; liquor minimum temperature

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乌海职业技术学院毕业设计

54 ℃; Gas preheating temperature 69.6 ℃; saturator central gas pipe diameter 1530 mm; gas inlet tube diameter of 1090 mm; saturated with a diameter of 5000mm; saturator height of 7740 mm; addition to acid inlet pipe diameter 1660 mm; addition to acid with a diameter of 2720 mm ; In addition to acid inside the outlet pipe section in the height of 4150 mm; dryer fluidized bed area of 0.778 square meters; dryer diameter of 1000 mm; dryer overflow gate height 388 mm; recovered from the reactor volume of pyridine base 18.355kg / h; liquor handling capacity 1087.29l/ h; ammonia and the device assigned to the mass fraction of 95.7%; in and with a diameter of 1220 mm; in and device cylinder height 1220 mm; in and the device overall height 1775 mm; holding area 7.97 ㎡; equipment quality 756.03kg .

Key words: nitrogen; ammonia; sulfuric acid; saturator law; liquor; ammonium sulfate: crystal: and in devices; pyridine

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乌海职业技术学院毕业设计

目录

第一章 总 论 ..................................... 6 1.1 概述 .............................................. 6 1.2 文献综述 .......................................... 6 1.2.1 用硫酸回收氨的生产工艺原理 .................... 7 1.2.2 从硫酸铵母液中制取粗轻吡啶工艺原理 ............ 8 1.3 设计条件及要求 ................................... 10 1.4 工艺流程的确定 ................................... 11 第二章 回收氨的工艺流程 ............................ 12 第三章 硫酸铵生产的影响因素及其控制 .................. 14 3.1 母液酸度 ......................................... 14 3.2 母液温度 ......................................... 15 3.3 母液搅拌 ......................................... 16 3.4 离心分离和水洗 ................................... 16 3.5 杂质 ............................................. 18 3.6 晶比 ............................................. 19 第四章 回收氨时物料平衡和热量平衡的计算 .............. 20 4.1 物料衡算 ......................................... 20 4.1.1氨的平衡及硫酸用量的计算和硫酸铵产量的计算 ..... 20 4.1.2 水平衡及母液温度的确定 ........................ 21 4.2 热量衡算 ......................................... 23 4.2.1输入热量 ...................................... 23

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乌海职业技术学院毕业设计

4.2.2 输出热量 ...................................... 26 第五章 硫酸铵生产的主设备计算 ....................... 28 5.1 饱和器 ........................................... 28 5.2 除酸器 ........................................... 30 5.3 干燥器 ........................................... 32 5.4 结晶槽 ........................................... 37 第六章 中和器法提取粗轻吡啶工艺流程 .................. 39 第七章 影响粗轻吡啶生产的因素及其控制 ................ 41 7.1 吸收阶段 ......................................... 41 7.2 中和及粗轻吡啶分离阶段 ........................... 42 第八章 中和器的物料平衡工艺计算 ..................... 43 8.1 母液处理量 ....................................... 43 8.2 分凝器后氨气分配给中和器的质量分数 ............... 44 第九章 回收粗轻吡啶的主要设备计算 .................... 45 9.1 中和器 ........................................... 45 9.2 冷凝冷却器 ....................................... 46 9.3 沉淀槽 ........................................... 46 第十章 设计一览表 .................................. 47 参考文献 .......................................... 48 设计体会与收获 ..................................... 49 致谢 .............................................. 50

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