CN101929791B - 大产量高纯氮设备 - Google Patents

大产量高纯氮设备 Download PDF

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CN101929791B
CN101929791B CN201010257170XA CN201010257170A CN101929791B CN 101929791 B CN101929791 B CN 101929791B CN 201010257170X A CN201010257170X A CN 201010257170XA CN 201010257170 A CN201010257170 A CN 201010257170A CN 101929791 B CN101929791 B CN 101929791B
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heat exchanger
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林序飞
徐爱松
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SUZHOU OXYGEN PLANT CO., LTD.
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    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
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    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
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    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

Abstract

本发明提供一种大产量高纯氮设备，包括：预处理系统，纯化系统和分馏塔，所述预处理系统包括依次连接的过滤器、空气压缩机和预冷机；所述分馏塔包括透平膨胀机，以及精馏塔和冷凝蒸发器，所述精馏塔包括上塔和下塔，所述纯化系统的出口经管路连接到下塔的空气入口，该管路经过主换热器；所述下塔还设有用于富氧液空出口，所述预处理系统包括两组并联的依次连接的过滤器、空气压缩机和预冷机，本发明通过将富氧的管路、原料空气的管路、氮气的管路同时连接至主换热器，使得富氧和氮气的冷量得到充分利用，节能环保。

Description

大产量高纯氮设备
技术领域
本发明涉及一种大产量高纯氮设备，尤其涉及一种采用低温精馏的方法生产高纯氮的设备。
背景技术
当今世界科技与经济快速发展，各行各业对氮的需求急增，用量越来越大，促使空分设备越造越大，工艺流程越来越多。高纯氮设备的应用也越来越广，产品氮压力、纯度要求各有不同。需要针对不同的应用场合，定制符合其需求的高纯氮设备。
目前的高纯氮设备主要采用低温精馏的方法生产高纯氮。精馏作为一种传统的分离提纯手段已有上百年的历史，它被广泛应用于冶金、化工、玻璃、电子等各个行业领域。高纯氮设备的原料是空气，生产方法主要是低温精馏，生产过程中主要消耗的是电能。现有的高纯氮设备占地面积大，能耗高。
发明内容
本发明的目的是提供一种占地小，能耗低的大产量高纯氮设备。
本发明的目的通过提供以下技术方案来实现：
一种大产量高纯氮设备，包括：通过管路互相连接的预处理系统，纯化系统和分馏塔，所述预处理系统包括依次连接的过滤器、空气压缩机和预冷机；所述分馏塔包括透平膨胀机，用于热交换的主换热器和过冷器，以及精馏塔和冷凝蒸发器，所述精馏塔包括上塔和下塔，所述纯化系统的出口经管路连接到下塔的空气入口，该管路经过主换热器；所述下塔还设有用于供精馏产生的富氧液空流出的富氧液空出口，所述富氧液空出口经管路连接到所述纯化系统，该管路经过主换热器；所述上塔设有氮气出口，该出口连接的管路经过主换热器，所述预处理系统包括两组并联的依次连接的过滤器、空气压缩机和预冷机。
进一步的，所述预冷机包括分离冷凝水份的水分离器。
进一步的，所述预冷机内设置有板翅式换热器。
进一步的，所述纯化系统包括分子筛吸附器和电加热器。
进一步的，所述主换热器包括主换热器上部和主换热器下部。
进一步的，所述富氧液空出口连接的管路依次经过过冷器、冷凝蒸发器、主换热器下部、透平膨胀机、过冷器、主换热器下部、主换热器上部，最后连接到纯化系统。
进一步的，所述富氧液空出口连接的管路连接到纯化系统的电加热器。
本发明通过设置高效率的预冷机，减小了占地面积，通过将富氧的管路、原料空气的管路、氮气的管路同时连接至主换热器，使得富氧和氮气的冷量得到充分利用，节能环保；同时将富氧送入膨胀机进行制冷，结构合理、节约物料，流程配置简单。
附图说明
下面结合附图对本发明作进一步说明：
图1为本发明的具体实施例的结构示意图。
1    空气过滤器          15    分馏塔
3    空气压缩机          17    透平膨胀机
5    预冷机              19    主换热器上部
7    纯化系统            21    主换热器下部
9    分子筛吸附器        23    过冷器
11   电加热器            25    精馏塔
13   消音器              27    冷凝蒸发器
具体实施方式
本发明的原理是利用空气中氧氮沸点的不同，采用低温精馏的方法生产高纯度氮气。
以下参照附图说明本发明的具体实施例。
如图1，本发明的大产量高纯氮设备主要包括通过管路相互连接的预处理系统，纯化系统7和分馏塔15。
所述的预处理系统包括通过管路互相连接的过滤器1、空气压缩机3，和预冷机5。预冷机5采用氟利昂预冷机组将空气冷却至5~10℃，通过水分离器分离出被冷凝的水份，减小纯化系统的负荷，使纯化系统的吸附效果更好，保证设备连续安全运行周期≥1年的要求。该预冷机5中的冷媒蒸发器选用了高效板翅式换热器，设备体积小，占地面积小，阻力降小，换热效率高。确保冷却效果，使预冷机组在最佳效率下工作。这样在降低预冷机5功耗的同时降低了吸附剂再生的能耗，有利于节能。
预处理系统包括两组并联的依次连接的过滤器1、空气压缩机3，和预冷机5。
所述的纯化系统7主要包括两个分子筛吸附器9和两个电加热器11。由于预冷机5的采用，使得分子筛吸附器9吸附水分需要的吸附剂用量减少，可采用立式单层床结构形式。分子筛吸附器9使用部分分子筛吸附空气中余留的水份，大部分分子筛充分发挥其吸附CO2及CnHm的功效，纯化器可将空气中CO2及H2O的含量脱除至1PPm。分子筛吸附器采用正反流流通能力相近的且具备良好调节性能的均压阀门，保证装置再生过程中工况的相对稳定。两台分子筛吸附器9均用时序程序控制，其中均压阀采用分段控制，减少分子筛均压过程引起的上塔波动。污氮放空阀采用预开式控制，减少分子筛系统切换引起的精馏塔25的上塔波动。电加热管形式有U型管、棒状、管束等结构。
所述的分馏塔15主要包括通过管路相互连通的两个相互并联的透平膨胀机17、用于热交换的主换热器和过冷器26，精馏塔25，冷凝蒸发器27。其中主换热器包括主换热器上部19和主换热器下部21。精馏塔25包括上塔和下塔。下塔采用高效筛板塔，提升了氮气提取率，提取率的提高使得生产相同产量相同纯度氮气所需要的空气量减少，从而极大地降低了能耗。冷凝蒸发器27采用干式主冷，较为安全。
以下详述高纯氮的制备流程。其主要包括：原料空气压缩——空气预冷干燥——空气的净化——空气的冷却——低温精馏——废气膨胀制冷和产品复热输出。
原料空气经空气过滤器1过滤掉灰尘等杂质，然后进入空气压缩机3压缩到一定的压力后进入预冷机5，预冷机5对输入空气进行冷却干燥后，将其输出到纯化系统7。
空气进入到纯化系统7的两个分子筛吸附器9中，清除掉空气中的水、二氧化碳、乙炔以及其他碳氢化合物。经过进一步净化的原料空气输出到分馏塔15。
原料空气首先通过原料空气管路进入主换热器，主换热器还穿设有富氧管路和氮气管路。通过原料空气管路，原料空气依次经过主换热器上部19和主换热器下部21，和经过富氧管路和氮气管路流经主换热器的富氧和纯氮进行热交换，被其冷却后从精馏塔25的下塔下部的空气入口进入精馏塔25。在精馏塔25中，原料空气被分离为下塔底部的富氧液空和上塔顶部的高纯氮气。高纯氮气的一部分作为产品氮气直接从上塔的顶部氮气开口输出，经过氮气管路进入主换热器与原料空气进行热交换，将其冷却，本身被复热后作为产品氮气输出。高纯氮气的另一部分从上塔的顶部开口经管路输出到冷凝蒸发器27，被流经冷凝蒸发器27的富氧液空冷凝成为液氮，作为精馏塔25的回流液经管路回流到精馏塔25的上塔，由上塔上的液氮入口进入上塔。
下塔底部的富氧液空从下塔下部的富氧液空出口输出，经富氧管路流经过冷器23后进入冷凝蒸发器27进行热交换，升温后流入主换热器下部21回收部分冷量，然后进入透平膨胀机17，在透平膨胀机17中进行膨胀制冷，膨胀后的富氧气流从透平膨胀机17输出，进入过冷器23中与富氧液空过冷后再次进入主换热器进行热交换，将原料空气冷却，然后流入纯化系统7的电加热器11，随之输入分子筛吸附器9作为再生气体，透平膨胀机17中多余的富氧气经一个消音器13放出到空气中。
在本实施方式中精馏塔25得到的富氧液空和氮气的冷量均通过主换热器用于冷却原料空气，能量利用率高。
需要理解到的是：上述说明并非是对本发明的限制，在本发明构思范围内，所进行的添加、变换、替换等，也应属于本发明的保护范围。

Claims (7)

1.一种大产量高纯氮设备，包括：通过管路互相连接的预处理系统，纯化系统和分馏塔，所述预处理系统包括依次连接的过滤器、空气压缩机和预冷机；所述分馏塔包括透平膨胀机，用于热交换的主换热器和过冷器，以及精馏塔和冷凝蒸发器，所述精馏塔包括上塔和下塔，所述纯化系统的出口经管路连接到下塔的空气入口，该管路经过主换热器；所述下塔还设有用于供精馏产生的富氧液空流出的富氧液空出口，所述富氧液空出口经管路连接到所述纯化系统，该管路经过主换热器；所述上塔设有氮气出口，该出口连接的管路经过主换热器，其特征在于：所述预处理系统包括两组并联的依次连接的过滤器、空气压缩机和预冷机。
2.根据权利要求1所述的大产量高纯氮设备，其特征在于，所述预冷机包括分离冷凝水份的水分离器。
3.根据权利要求2所述的大产量高纯氮设备，其特征在于，所述预冷机内设置有板翅式换热器。
4.根据权利要求1所述的大产量高纯氮设备，其特征在于，所述纯化系统包括分子筛吸附器和电加热器。
5.根据权利要求1所述的大产量高纯氮设备，其特征在于，所述主换热器包括主换热器上部和主换热器下部。
6.根据权利要求5所述的大产量高纯氮设备，其特征在于，所述富氧液空出口连接的管路依次经过过冷器、冷凝蒸发器、主换热器下部、透平膨胀机、过冷器、主换热器下部、主换热器上部，最后连接到纯化系统。
7.根据权利要求6所述的大产量高纯氮设备，其特征在于，所述富氧液空出口连接的管路连接到纯化系统的电加热器。
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