CN114739117B - 一种使用单个精馏塔生产纯氮的装置及其使用方法 - Google Patents

一种使用单个精馏塔生产纯氮的装置及其使用方法 Download PDF

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CN114739117B
CN114739117B CN202210427841.5A CN202210427841A CN114739117B CN 114739117 B CN114739117 B CN 114739117B CN 202210427841 A CN202210427841 A CN 202210427841A CN 114739117 B CN114739117 B CN 114739117B
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CN114739117A (zh
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劳利建
姚蕾
李政辰
彭旭东
蒋云云
谭芳
韩一松
郑泽楠
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Hang Yang Group Co ltd
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Abstract

一种使用单个精馏塔生产纯氮的装置及其使用方法，该装置由空压机、预冷纯化系统，循环氮气增压机、高低温膨胀机制冷系统及冷箱系统组成，所述空压机前方设有空气过滤器，后方设置预冷纯化系统，空气通过空气过滤器进入空气透平压缩机内压缩至约4.5bar后，送入预冷纯化系统。空气在预冷纯化系统内经空冷塔冷却，分子筛除杂后，进入冷箱系统。空气经板式换热器冷却至接近饱和后，进入低温精馏塔精馏后获得低压氮气及液空，该股低压氮气通过换热器复热出冷箱，一部分作为产品，一部分进入循环氮气压缩机。本方法具有能够大幅度提高低温精馏制氮装置的提取率，降低纯氮装置的能耗等优点。

Description

一种使用单个精馏塔生产纯氮的装置及其使用方法
技术领域
本发明涉及的是一种使用单个精馏塔生产纯氮的装置及其使用方法，更具体的说，通过带冷凝器及蒸发器的精馏塔、循环氮气压缩机与膨胀机组的高效耦合来生产大量液氮与多规格氮气的节能方法与装置。
背景技术
氮气占大气组分的78%左右，其性质不活泼，具有化学惰性，是一种应用领域广泛的工业气体，被广泛应用在化工生产、装备制造、食品保鲜、激光切割等领域。目前的纯氮生产设备主要采用低温精馏方法，低温精馏分离作为空分领域应用范围最广的方法已有上百年的历史，目前广泛应用于冶金、化工、玻璃、电子等各个行业领域。
随着各行各业技术的快速发展，生产过程中对氮气的需求量迅速增加。同时伴随着产业多元化的发展趋势，生产工艺的多样化也导致生产对氮气产品的规格需求也越来越多，大量终端用户对氮气的需求量较少，纯度要求又极高。因此，能够适应大量及多规格氮气提取，同时能大量生产方便运输的纯液氮，并能有效降低能耗的空分设备工艺流程应用前景广泛。
发明内容
本发明的目的在于提供一种使用单个精馏塔生产纯氮的装置及其使用方法，此方法可以大幅度提高精馏塔的提取率，减小原料气体的加工量，从而有效降低氮气制备的能耗。本发明的目的是通过如下技术方案来完成的：一种使用单个精馏塔生产纯氮的装置，该装置由空气透平压缩机、预冷纯化系统、循环氮气压缩机、低温精馏塔、高低温膨胀机制冷系统及冷箱系统组成，所述空气透平压缩机前方设有空气过滤器，后方设置预冷纯化系统，空气通过空气过滤器进入空气透平压缩机内压缩至约4.5bar后，送入预冷纯化系统，空气在预冷纯化系统内经空冷塔冷却，分子筛除杂后，进入冷箱系统，空气经板式换热器冷却至接近饱和后，进入低温精馏塔精馏后获得低压氮气及液空，该股低压氮气通过换热器复热出冷箱，分为两部分，一部分作为低压氮气产品送入用户产品氮气管网；一部分进入循环氮气压缩机继续增压，氮气经循环氮气压缩机加压后分为四部分：第一部分从循环氮气压缩机一级叶轮后中抽出后分为两股，一股作为低温精馏塔底部设置的蒸发器热源，一股抽出作为产品；第二部分从循环氮气压缩机末级抽出作为产品；第三部分从循环氮气压缩机末级抽出返回换热器作为高温膨胀量；第四部分去膨胀机增压端继续增压，去膨胀机增压端继续增压的氮气经过低温膨胀机增压端及低温膨胀机增压端后冷却器增压冷却后，继续进入高温膨胀机增压端及高温膨胀机增压端后冷却器增压冷却后分为两股，一股作为高压氮气去板式换热器冷却后从冷端抽出，节流进入气液分离器，一股作为低温膨胀量去板式换热器冷却后从板式换热器下段抽出，去低温膨胀机膨胀端，膨胀后带液氮气去气液分离器；
其中所述低温精馏塔底部获得低压富氧液空，顶部获得低压氮气，富氧液空节流至常压后送入冷凝蒸发器的蒸发侧，与低温精馏塔顶部的低压氮气换热后气化得到污氮气；
所述循环氮气压缩机一级叶轮后抽出的氮气经板式换热器冷却至饱和温度后，送入精馏塔底部蒸发器冷凝侧，与低温精馏塔精馏产生的低压富氧液空换热后，冷凝成液氮，冷凝后的液氮节流进入低温精馏塔顶部参与精馏，蒸发器蒸发侧蒸发的液空蒸汽作为低压精馏塔内的上升气，参与精馏。
作为优选：所述气液分离器中的液氮分为两部分，一部分作为回流液氮，返流回低压精馏塔参与精馏，一部分去液氮过冷器，过冷后的液氮分为两部分，一部分作为液氮产品，一部分作为过冷器冷源氮气节流至常压，返流与液氮过冷器的液氮换热后，与污氮气并流得到污氮气，所述污氮气经板式换热器复热后出冷箱，分为两股，一股作为分子筛再生气源去再生加热器，一股作为水冷塔用污氮气。
一种使用单个精馏塔生产纯氮的装置的使用方法，包括如下步骤：
a）来自大气的原料空气作为原料气体，经过空气透平压缩机增压，得到高温气体；高温气体经预冷纯化系统冷却吸附后，得到低压空气；
b）低压空气进入冷箱内的主换热器，被返流气体冷却至饱和温度后进入低压精馏塔参与精馏；
c）经低压精馏塔精馏后，在低压精馏塔顶部获得低压氮气，在低压精馏塔底部获得富氧液空；富氧液空节流至常压，送入冷凝蒸发器蒸发侧；低压氮气直接进入主换热器，与正流低压空气进行热交换，复热到常温后送出冷箱；
d）进入冷凝蒸发器蒸发侧的富氧液空与精馏塔顶部的低压氮气换热后汽化的到污氮气，污氮气送入主换热器复热后出冷箱，一部分去分子筛作为再生气源，一部分去水冷塔冷却循环水；
e）出冷箱低压氮气一部分作为低压氮气产品，其余去循环氮气压缩机继续增压；
f）低压氮气经循环氮气压缩机压缩后，分为四部分，第一部分从增压机一级叶轮后中抽后分为两股，一股作为蒸发器热源，一股中抽作为产品；第二部分从循环氮气压缩机末级抽出作为产品；第三部分从循环氮气压缩机末级抽出返回换热器作为高温膨胀量，经板式换热器冷却后去高温膨胀机膨胀端膨胀后，返流回板式换热器复热出冷箱后去循环氮压机入口；第四部分去膨胀机增压端继续增压；
g）去膨胀机增压端继续增压的氮气经过低温膨胀机增压端及低温膨胀机增压端后冷却器增压冷却后，继续进入高温膨胀机增压端及高温膨胀机增压端后冷却器增压冷却后分为两股，一股作为高压氮气去板式换热器冷却后从冷端抽出，节流进入气液分离器，一股作为低温膨胀量去板式换热器冷却后从板式下段抽出，去低温膨胀机膨胀端，膨胀后带液氮气去气液分离器；
h）气液分离器分离得到的低压氮气与下塔顶部抽取的低压氮气并流后去主换热器复热，分离得到的低压液氮一部分送入下塔顶部参与精馏，一部分作为产品液氮，送入液氮过冷器，与返流的常压氮气换热后出冷箱；
i）液氮过冷器中返流的常压氮气由产品液氮中抽取一部分节流至常压获得，出过冷器的常压氮气与冷凝蒸发器蒸发侧的常压污氮气并流，去主换热器复热出冷箱。
本发明具有以下特点：
本发明采用的单塔精馏方法能够有效提高单塔制氮装置的提取率，减少制氮装置的能耗。在流程布置方面更是有极大的自由度，可根据不同气体和液体氮产品的规格对循环氮气压缩机及膨胀机组进行优化配置，达到最佳能耗点。单个精馏塔操作灵活，调整快捷的特点也得到保留。
附图说明
图1是本发明的结构示意图。
具体实施方式
下面将结合附图对本发明作详细的介绍：如图1所示，一种使用单个精馏塔生产纯氮的装置，该装置由空气透平压缩机3、预冷纯化系统、循环氮气压缩机21、低温精馏塔15、高低温膨胀机制冷系统及冷箱系统组成，所述空气透平压缩机3前方设有空气过滤器2，后方设置预冷纯化系统，空气通过空气过滤器2进入空气透平压缩机3内压缩至约4.5bar后，送入预冷纯化系统，空气在预冷纯化系统内经空冷塔4冷却，分子筛12除杂后，进入冷箱系统，空气经板式换热器14冷却至接近饱和后，进入低温精馏塔15精馏后获得低压氮气及液空，该股低压氮气通过板式换热器14复热出冷箱，分为两部分，一部分作为低压氮气产品20送入用户产品氮气管网；一部分进入循环氮气压缩机21继续增压，氮气经循环氮气压缩机21加压后分为四部分：第一部分从循环氮气压缩机一级叶轮后中抽出后分为两股，一股作为低温精馏塔15底部设置的蒸发器24热源，一股抽出作为产品；第二部分从循环氮气压缩机末级抽出作为产品；第三部分从循环氮气压缩机末级抽出返回板式换热器14作为高温膨胀量；第四部分去膨胀机增压端继续增压，去膨胀机增压端继续增压的氮气经过低温膨胀机增压端31及低温膨胀机增压端后冷却器32增压冷却后，继续进入高温膨胀机增压端33及高温膨胀机增压端后冷却器34增压冷却后分为两股，一股作为高压氮气去板式换热器14冷却后从冷端抽出，节流进入气液分离器38，一股作为低温膨胀量去板式换热器14冷却后从板式换热器14下段抽出，去低温膨胀机膨胀端36，膨胀后带液氮气去气液分离器38；其中所述低温精馏塔15底部获得低压富氧液空17，顶部获得低压氮气16，富氧液空17节流至常压后送入冷凝蒸发器18的蒸发侧，与低温精馏塔15顶部的低压氮气换热后气化得到污氮气19；所述循环氮气压缩机一级叶轮后抽出的氮气经板式换热器14冷却至饱和温度后，送入精馏塔底部蒸发器24冷凝侧，与低温精馏塔15精馏产生的低压富氧液空17换热后，冷凝成液氮，冷凝后的液氮节流进入低温精馏塔15顶部参与精馏，蒸发器24蒸发侧蒸发的液空蒸汽作为低压精馏塔内的上升气，参与精馏。
所述气液分离器38中的液氮41分为两部分，一部分作为回流液氮42，返流回低压精馏塔参与精馏，一部分去液氮过冷器46，过冷后的液氮44分为两部分，一部分作为液氮产品45，一部分作为过冷器冷源氮气节流至常压，返流与液氮过冷器46的液氮换热后，与污氮气19并流得到污氮气37，所述污氮气37经板式换热器14复热后出冷箱，分为两股，一股作为分子筛再生气源48去再生加热器49，一股作为水冷塔用污氮气8。
一种应用上述的使用单个精馏塔生产纯氮的装置的使用方法，包括如下步骤：
a）来自大气的原料空气作为原料气体，经过空气透平压缩机增压，得到高温气体；高温气体经预冷纯化系统冷却吸附后，得到低压空气；
b）低压空气进入冷箱内的主换热器，被返流气体冷却至饱和温度后进入低压精馏塔参与精馏；
c）经低压精馏塔精馏后，在低压精馏塔顶部获得低压氮气，在低压精馏塔底部获得富氧液空；富氧液空节流至常压，送入冷凝蒸发器蒸发侧；低压氮气直接进入主换热器，与正流低压空气进行热交换，复热到常温后送出冷箱；
d）进入冷凝蒸发器蒸发侧的富氧液空与精馏塔顶部的低压氮气换热后汽化的到污氮气，污氮气送入主换热器复热后出冷箱，一部分去分子筛作为再生气源，一部分去水冷塔冷却循环水；
e）出冷箱低压氮气一部分作为低压氮气产品，其余去循环氮气压缩机继续增压；
f）低压氮气经循环氮气压缩机压缩后，分为四部分，第一部分从增压机一级叶轮后中抽后分为两股，一股作为蒸发器热源，一股中抽作为产品；第二部分从循环氮气压缩机末级抽出作为产品；第三部分从循环氮气压缩机末级抽出返回换热器作为高温膨胀量，经板式换热器冷却后去高温膨胀机膨胀端膨胀后，返流回板式换热器复热出冷箱后去循环氮压机入口；第四部分去膨胀机增压端继续增压；
g）去膨胀机增压端继续增压的氮气经过低温膨胀机增压端31及低温膨胀机增压端后冷却器32增压冷却后，继续进入高温膨胀机增压端33及高温膨胀机增压端后冷却器34增压冷却后分为两股，一股作为高压氮气去板式换热器14冷却后从冷端抽出，节流进入气液分离器38，一股作为低温膨胀量去板式换热器14冷却后从板式下段抽出，去低温膨胀机膨胀端36，膨胀后带液氮气去气液分离器38；
h）气液分离器分离得到的低压氮气与下塔顶部抽取的低压氮气并流后去主换热器复热，分离得到的低压液氮一部分送入下塔顶部参与精馏，一部分作为产品液氮，送入液氮过冷器，与返流的常压氮气换热后出冷箱；
i）液氮过冷器中返流的常压氮气由产品液氮中抽取一部分节流至常压获得，出过冷器的常压氮气与冷凝蒸发器蒸发侧的常压污氮气并流，去主换热器复热出冷箱。
本发明提供一种可以实施的适合于需要多种规格氮气（4bar(A)/10bar(A)/30bar(A)）及大量液氮的单塔氮气循环低温精馏制氮方法。该方法克服了现有的单塔精馏法制氮装置在制取氮气时，氮气的提取率较低，规格较为单一，能耗较高的不足，调整了精馏塔的液气比值，充分利用了精馏塔的分离能力，大幅提制氮空分装置的提取率，从而显著降低单位产品的能耗指标。

Claims (3)

1.一种使用单个精馏塔生产纯氮的装置，该装置由空气透平压缩机（3）、预冷纯化系统、循环氮气压缩机（21）、低温精馏塔（15）、高低温膨胀机制冷系统及冷箱系统组成，其特征在于：所述空气透平压缩机（3）前方设有空气过滤器（2），后方设置预冷纯化系统，空气通过空气过滤器（2）进入空气透平压缩机（3）内压缩至4.5bar后，送入预冷纯化系统，空气在预冷纯化系统内经空冷塔（4）冷却，分子筛（12）除杂后，进入冷箱系统，空气经板式换热器（14）冷却至接近饱和后，进入低温精馏塔（15）精馏后获得低压氮气及液空，该股低压氮气通过板式换热器（14）复热出冷箱，分为两部分，一部分作为低压氮气产品（20）送入用户产品氮气管网；一部分进入循环氮气压缩机（21）继续增压，氮气经循环氮气压缩机（21）加压后分为四部分：第一部分从循环氮气压缩机一级叶轮后中抽出后分为两股，一股作为低温精馏塔（15）底部设置的蒸发器（24）热源，一股抽出作为产品；第二部分从循环氮气压缩机末级抽出作为产品；第三部分从循环氮气压缩机末级抽出返回板式换热器（14）作为高温膨胀量；第四部分去膨胀机增压端继续增压，去膨胀机增压端继续增压的氮气经过低温膨胀机增压端（31）及低温膨胀机增压端后冷却器（32）增压冷却后，继续进入高温膨胀机增压端（33）及高温膨胀机增压端后冷却器（34）增压冷却后分为两股，一股作为高压氮气去板式换热器（14）冷却后从冷端抽出，节流进入气液分离器（38），一股作为低温膨胀量去板式换热器（14）冷却后从板式换热器（14）下段抽出，去低温膨胀机膨胀端（36），膨胀后带液氮气去气液分离器（38）；
其中所述低温精馏塔（15）底部获得低压富氧液空（17），顶部获得低压氮气（16），富氧液空（17）节流至常压后送入冷凝蒸发器（18）的蒸发侧，与低温精馏塔（15）顶部的低压氮气换热后气化得到污氮气（19）；
所述循环氮气压缩机一级叶轮后抽出的氮气经板式换热器（14）冷却至饱和温度后，送入精馏塔底部蒸发器（24）冷凝侧，与低温精馏塔（15）精馏产生的低压富氧液空（17）换热后，冷凝成液氮，冷凝后的液氮节流进入低温精馏塔（15）顶部参与精馏，蒸发器（24）蒸发侧蒸发的液空蒸汽作为低压精馏塔内的上升气，参与精馏。
2.根据权利要求1所述的使用单个精馏塔生产纯氮的装置，其特征在于：所述气液分离器（38）中的液氮（41）分为两部分，一部分作为回流液氮（42），返流回低压精馏塔参与精馏，一部分去液氮过冷器（46），过冷后的液氮（44）分为两部分，一部分作为液氮产品（45），一部分作为过冷器冷源氮气节流至常压，返流与液氮过冷器（46）的液氮换热后，与冷凝蒸发器蒸发侧的污氮气（19）并流得到污氮气（37），并流后的污氮气（37）经板式换热器（14）复热后出冷箱，分为两股，一股作为分子筛再生气源（48）去再生加热器（49），一股作为水冷塔用污氮气（8）。
3.根据权利要求1-2任意一项权利要求所述的使用单个精馏塔生产纯氮的装置的使用方法，其特征在于：包括如下步骤：
a）来自大气的原料空气作为原料气体，经过空气透平压缩机增压，得到高温气体；高温气体经预冷纯化系统冷却吸附后，得到低压空气；
b）低压空气进入冷箱内的主换热器，被返流气体冷却至饱和温度后进入低压精馏塔参与精馏；
c）经低压精馏塔精馏后，在低压精馏塔顶部获得低压氮气，在低压精馏塔底部获得富氧液空；富氧液空节流至常压，送入冷凝蒸发器蒸发侧；低压氮气直接进入主换热器，与正流低压空气进行热交换，复热到常温后送出冷箱；
d）进入冷凝蒸发器蒸发侧的富氧液空与精馏塔顶部的低压氮气换热后汽化的到污氮气，污氮气送入主换热器复热后出冷箱，一部分去分子筛作为再生气源，一部分去水冷塔冷却循环水；
e）出冷箱低压氮气一部分作为低压氮气产品，其余去循环氮气压缩机继续增压；
f）低压氮气经循环氮气压缩机压缩后，分为四部分，第一部分从增压机一级叶轮后中抽后分为两股，一股作为蒸发器热源，一股中抽作为产品；第二部分从循环氮气压缩机末级抽出作为产品；第三部分从循环氮气压缩机末级抽出返回换热器作为高温膨胀量，经板式换热器冷却后去高温膨胀机膨胀端膨胀后，返流回板式换热器复热出冷箱后去循环氮压机入口；第四部分去膨胀机增压端继续增压；
g）去膨胀机增压端继续增压的氮气经过低温膨胀机增压端（31）及低温膨胀机增压端后冷却器（32）增压冷却后，继续进入高温膨胀机增压端（33）及高温膨胀机增压端后冷却器（34）增压冷却后分为两股，一股作为高压氮气去板式换热器（14）冷却后从冷端抽出，节流进入气液分离器（38），一股作为低温膨胀量去板式换热器（14）冷却后从板式下段抽出，去低温膨胀机膨胀端（36），膨胀后带液氮气去气液分离器（38）；
h）气液分离器分离得到的低压氮气与下塔顶部抽取的低压氮气并流后去主换热器复热，分离得到的低压液氮一部分送入下塔顶部参与精馏，一部分作为产品液氮，送入液氮过冷器，与返流的常压氮气换热后出冷箱；
i）液氮过冷器中返流的常压氮气由产品液氮中抽取一部分节流至常压获得，出过冷器的常压氮气与冷凝蒸发器蒸发侧的常压污氮气并流，去主换热器复热出冷箱。
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