CN1152350A - 高效率氮气发生器 - Google Patents

高效率氮气发生器 Download PDF

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CN1152350A
CN1152350A CN96190424A CN96190424A CN1152350A CN 1152350 A CN1152350 A CN 1152350A CN 96190424 A CN96190424 A CN 96190424A CN 96190424 A CN96190424 A CN 96190424A CN 1152350 A CN1152350 A CN 1152350A
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nitrogen
rich
oxygen
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compressor
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B·哈
M·图尼
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Liquid Air Engineering Corp Canada
Liquid Air Engineering Corp USA
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Abstract

公开了一种用单塔式装置实现氮高效率生产的工艺与设备，来自蒸馏柱(20)的富氧液部分气化分成液体与蒸气相，该液体在第二再沸器/冷凝器(60)气化后发生气体膨胀，为氮的生产过程提供所需的冷冻条件，而有高氮含量的上述蒸发气体则经压缩后回到可使它与料气分离的蒸馏柱中，以得到更高的总体氮回收率。

Description

高效率氮气发生器
本发明涉及用冷冻蒸馏来实现氮高效生产的一种工艺和设备。
本领域的技术人员都熟悉用空气生产氮的许多工艺。生产氮时以氮为主要产品，在冷冻条件下用单塔对空气进行分离和利用富氧气体的膨胀对空气进行冷冻是众所周知的。
专利US-A-4,883,519介绍了利用废富氧蒸气的膨胀来生产氮的基本方法与设备。在此文中描述了根据独立权利要求的前序部分的方法与设备。
在专利US-A-4,883,519中，第一冷凝器的富氮蒸气是用物料空气在热交换器的上游压缩的，为此它需使用复杂的且非标准型的压缩机。
因为富氮蒸气是在主交换器的上游被压缩的，因此所有的阀门、管线、纯化***、冷却器、蒸馏塔与热交换器的尺寸都必须由主要物料空气和富氮蒸气构成的总的压缩气体容积来进行计算。
本发明旨在降低设置的投资、生产的能耗。它还希望比现有技术能减小空气纯化***的尺寸。
从专利EP-A-0,607,979得知，也可由物料空气的膨胀来实现单塔式氮气发生器的冷冻要求。
本发明提供了空气冷冻分离生产高纯氮的工艺程序。它包括：(a)向蒸馏塔的第一区段提供压缩、干燥、清洁和冷却的空气料气；(b)将所述料气在上述蒸馏塔中分离为富氮蒸气与富氧液体，前者在该塔的上部，后者聚集在蒸馏塔底部；(c)在第一冷聚器中，通过上述富氮蒸气与至少一部分富氧液体的间接热交换，使部分富氮蒸气冷凝，而部分富氧液则气化形成富氧液和第二富氮蒸气；(d)在第二冷凝器中，通过至少一部分所述富氧液与至少一部分所述富氮蒸气的间接热交换，使至少一部分所述富氧液氧化，产生富氮冷凝液与废的蒸气；(e)将至少一部分所述第二富氮蒸气循环到循环压缩机，形成压缩了的循环气体；其特性在于它包括(f)将至少一部分上述压缩了的循环气体供给蒸馏塔的第二区段，该区段与蒸馏塔的第一区段相隔至少有一个理论塔板数。
优选地，上述的循环压缩机为冷压缩机，进入该冷压缩机的富氧蒸气温度在-50℃以下。
上述的富氮蒸气的循环部分最好是另用一个压缩机压缩，而不是用主压缩机压缩。
本发明还提供了冷冻蒸馏生产氮的设备，它包括：(a)用料气蒸馏所得诸产品来使料气致冷的一个热交换器；(b)把所述料气分离成基本上为氮的蒸气与富氮液体的一个蒸馏塔以及使所述料气进入蒸馏塔第一区段的设施；(c)使所述富氧液蒸发形成富氧冷凝物和富氮循环流料的第一冷凝器，即通过使富氧液与至少一部分所述基本上为氮的蒸气热交换来蒸发；(d)排出上述富氧液并将它送往一个第二冷凝器的设施；(e)排出上述富氮循环蒸气并把它送到一个循环压缩机的设施；(f)在所述第二冷凝器中使所述富氧液气化的间接热交换器；(g)排出并发送上述废气体到所述热交换器的设施；(h)压缩上述循环富氮蒸气的压缩机；(i)把上述压缩的循环富氮蒸气送往所述蒸馏塔第二区段的设施；(j)将富氮蒸气送入所述热交换器，使进入热交换器的其他气体升温的设施，
其特征在于蒸馏塔第一区段与第二区段间分隔至少一个理论塔板数。
可以通过部分料气或蒸馏塔出来的富氧蒸气的一部分的膨胀实现氮生产过程所需的冷冻作用。
图1是介绍本发明的主要工艺流程和生产设备的一种实施方案的示意图。
图2是介绍本发明主要工艺流程、生产设备和包括耗散制动设施的另一种实施方案的示意图。
图1描述了本发明的最佳实施方案，空气料气2在主热交换器10得到冷却后由管线4送入蒸馏塔20。料气在进入蒸馏塔前经干燥并用吸收器、过滤器和附加的热交换器等众所周知的方法纯化。在单塔式蒸馏塔20的蒸馏区段17提取出氧，而在该区段上部产生富氮蒸气。在蒸馏塔20的底部，排出富氧液体6并使其与流入主热交换器10的其他物流热交换而过冷。此后富氧液流膨胀并通过管道7进入冷凝器段30。该第一冷凝器段30有一个第一再沸器/冷凝器50，这里有通过管线31由蒸馏塔来的第一部分富氮蒸气，它与富氧液间接热交换而冷凝。而氮的冷凝液则通过管线32作为回流液回到蒸馏塔，必要时这种氮的冷凝液可部分取出作为液氮产品。
在冷凝器段30的一部分富氧液气化，在其壳体产生液相和富氮的蒸气相。本发明中有不同组成的这两种物相都经过进一步处理，用来产生有高回收率的氮产品。第一冷凝器段30形成的液体经排出、至少部分膨胀由管线8进入有再沸器/冷凝器60的第二冷凝器段40。按本发明，从第一冷凝器壳体来的至少一部分富氧液与从蒸馏塔来的富氮蒸气产生间接热交换而在第二冷凝器40气化。该第二部分富氮蒸气是通过管线21进入再沸器/冷凝器60的，并在第二冷凝器40产生冷凝的富氮液，该富氮液通过管线22从冷凝器40排出，其中至少一部分由管线24作为回流液送往蒸馏塔，必要时，由管线23将液氮产品从第二冷凝器排出。需要时可由第一冷凝器产生的液氮，第二冷凝器产生的液氮或二者的混合液作为生产的液氮产品。
按本发明，气化的富氧物流41与其他物流热交换而升温产生了升温了的富氧物流42。升温了的富氧物流42的至少一部分在膨胀室80发生膨胀形成膨胀的废物流45，膨胀了的物流再进入主热交换器与其他物流发生热交换进一步升温，升温了的该物流作为废物流47排出去。
在第一冷凝器段30产生的蒸气经管线12排出并进入压缩机70，压缩后经管线13进入蒸馏塔。根据本发明，从冷凝器30排出的蒸气12比料气有较高的氧含量。因此优选它压缩后再循环进入蒸馏塔时，它的进口应比主料气由管线4进入蒸馏塔的进口至少应低一个理论塔板数的高度，一般所述循环物流含氧在25-29摩尔百分数，而所述废物流含氧量则大于46摩尔百分数。优选地，蒸馏塔的蒸馏区段19宜配置在主料气进口点与循环富氧物流返回蒸馏塔的进口点之间。
在本发明的优选实施方案中，膨胀器80与压缩机70是机械地相连结的，因此气体膨胀时释出的至少一部分能量可直接供压缩使用，压缩机70宜用冷压缩机，它与膨胀器80机械相连。在这种情况下，可使用能量吸收器89耗散进入膨胀器88的一部分物流42的膨胀能量，以维持整个过程的热平衡。图2中膨胀器80与88是合为一个膨胀器并与压缩机70连结的。这种情况下，该相连***的轴和一个制动器81相连接，以离散部分膨胀能而保持整个工作***的平衡。
气体氮产品由蒸馏塔20的顶部排放出去，经管线26送入主热交换器将它升温，此后便可由管道27接收气体氮产品。
在本发明方法和设备的众多优点中，其中的一个优点是冷凝器段30中可维持较高的压力，因为液体物流被排放，使得蒸发的物流中含较少的氧气。另外，如果冷凝器30在较高的压力下操作，可使该气体在压缩机70压缩时所需作的功减低，在同等量的输入功给压缩机70时可有较高流量的循环气流。在本发明方法中，循环气流的高流量与高的氮浓度可使本发明有高的氮回收率，根据这里讲述的本发明，本领域的技术人员对本发明其他优点的了解是不言而喻的，下面提供本发明实施的实例。
实例
按本发明提出的工艺，制造了一个氮的生产装置，它生产的氮含氧量不超过1ppm，产品氮输出的气压为124psia(磅/平方英寸)，流量为100,000SCFH(标准立方英尺/小时)。
60°F，132psia、173，549SCFH的干燥和纯净空气流(物流2)(实际上无氮与CO2)在通过管线4进入蒸馏塔17的中间区域前，首先进入热交换器10冷却到-268°F。
含氧量为39.77摩尔百分数、流量为132,519 SCFH的富氧液流通过管线6从蒸馏塔17的底部排出，在热交换器10过却到-277.6°F，经阀门膨胀后由物流7进入主蒸发器壳体30。含氧量为27.7摩尔百分数、流量为58.971 SCFH的富氧气态物流12在-279.4°F、74.9psia由主蒸发器30输出。物流12经循环升压器70压缩到129.8psia后送入蒸馏塔17的底部。送入主蒸发器30中的余量的富氧液通过物流8送入辅助蒸发器40，在57.75psia、-279.4°F气化。气态的富氧废物流41送入主热交换器10将其升温到-238°F，然后在透平机80与88膨胀后重新进入热交换器10，在此升温到55°F。该废物流47以73,548SCFH的流量排出，其中的含氧量为49.5摩尔百分数。
由蒸馏塔17顶部经物流26排出气体氮，它为-276.6F、126.4psia和流量100,000SCFH，在热交换器10升温到55°F后以124psia由物流27输送出去作为纯氮产品。
为了说明本发明的优点，我们将本工艺与专利US-A-4,966,002图4的工艺就料气的供求量作了模拟对比，在执行这种模拟对比时，使用了相似的生产要求、生产过程中的热漏、热交换器温度收聚(pinch)和蒸馏塔操作压力等条件。
与US-A-4,966,002中图4工艺对比的结果表明，本工艺供给冷箱(热交换器)的料气量可减少4.55％。
同样地本工艺与专利US-A-4,883,519的工艺对比结果如下：
                          US-A-4,883,51   本工艺废氮气流(物流47)氧含量(％)         40.7        49.5循环物流压力(psia)                 68          74.9循环物流(料气百分数)               17.25       34料气流量(塔中总供给量百分数)        85.3        74.6相对能耗                           100         90
因此，由上表可知本工艺能耗明显低于专利US-A-4,883,519的能耗。

Claims (16)

1.提出了一种通过冷冻分离从空气中生产高纯氮的方法，它包括：(a)给蒸馏塔(20)的第一区段提供一种压缩、干燥、纯净与冷却的空气料气；(b)在所述的蒸馏塔中将所述料气分离为在其顶部的富气蒸气和底部的富氧液体；(c)部分所述的富氮蒸气和部分所述富氧液体在第一冷凝器(50)间接热交换，使富氮蒸气冷凝，其中所述富氧液至少部分气化，生成富氧液和一种第二富氮蒸气；(d)至少部分的富氧液与至少部分所述富氮蒸氧在第二冷凝器(60)进行间接热交换，其中的至少部分所述富氧液气化，生成富氮冷凝液和废物流；(e)上述的第二富氮蒸气至少有部分循环到循环压缩机(70)，形成压缩的循环物流；
其特征在于该方法包括(f)将至少部分所述的压缩的循环物流加入所述蒸馏塔的第二蒸馏区段，该区段与其第一区段至少分隔有一个理论塔板数。
2.权利要求1的方法，其中至少有部分所述富氮冷凝液可取出作为液氮产品。
3.权利要求1的方法，其中从所述第二冷凝器得的所有所述富氮冷凝液都可作为回流液返回到蒸馏塔。
4.前述任一项权利要求的方法，其中在第一冷凝器(50)中的富氮蒸气冷凝液至少可部分取出作为液氮产品。
5.前述任一项权利要求的方法，其中所述的循环物流含有25-29摩尔百分数的氧，所述废物流含有高于46摩尔百分数的氧。
6.前述任一项权利要求的方法，包括至少有部分所述废物流或所述料气在膨胀器(80)发生膨胀，为所述生产过程提供所需的冷冻作用。
7.前述任一项权利要求的方法，其中所述的膨胀器(80)是与所述循环压缩机(70)机械相连的。
8.前述任一项权利要求的方法，其中所述压缩机(70)是一种冷压缩机，进入所述冷压缩机的所述富氧气体的温度至少低于-50℃。
9.前述任一项权利要求的方法，包括部分所述废物流在第二膨胀器(80)发生气体膨胀，第二膨胀器是与能量耗散器(81)机械相连的。
10.前述任一项权利要求的方法，其中所述的所有富氧冷凝液基本上都气化、升温，然后在所述膨胀器(80)发生膨胀。
11.前述任一项权利要求的方法，其中至少有部分所述料气在所述蒸馏塔(20)的抽提区(19)提取而产生至少部分所述富氧液体。
12.前述任一项权利要求的方法，其中所述的部分富氮蒸气是在压缩机(70)压缩，而不是在主空气压缩机压缩。
13.在冷冻条件下生产氮的设备，包括：(a)用料气蒸馏所得的产品来冷却料气的热交换器(10)；(b)将所述料气分离成基本上为氮的蒸气与富氧液的蒸馏塔(20)和将所述料气送入所述蒸馏塔(20)第一区段的设施；(c)将所述富氧液与部分基本上为氮的蒸气间接热交换的第一冷凝器(50)，它使所述富氧液气化生成富氧冷凝液和富氮的循环物流；(d)排出与发送所述富氧液到第二冷凝器(60)的设施(8)；(e)排出与发送所述富氮循环物流到循环压缩机(70)的设施；(f)在第二冷凝器中使所述富氧液蒸发的间接热交换设施；(g)排出与发送所述废物流到所述热交换器的设施(41)；(h)压缩所述富氮循环物流的压缩机(70)；(i)发送所述压缩的循环物流到蒸馏塔(20)第二区段的设施；(j)发送部分所述富氮蒸气到所述热交换器使其他物流升温的设施，
其特征在于第一与第二蒸馏段至少相隔一个理论塔板数。
14.权利要求13的设备，还包括：(a)从所述热交换器排出所述废物流并使其至少部分在至少一个膨胀器(80)中膨胀的设施或在膨胀器中膨胀至少部分料气的设施。
15.权利要求13或14的设备，还包括：(a)所述蒸馏塔(20)中低于第一区段的抽提设施(19)；(b)从所述压缩机(70)将压缩的富氮循环物流送入所述蒸馏塔中低于所述抽提段区域的设施。
16.权利要求12到15的任一项的设备，其中所述的压缩机(70)定位在一个冷箱内，以使压缩机与蒸馏塔(20)和/或热交换器(10)绝热的设施。
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