CN105637311B - 通过低温蒸馏分离空气的方法和装置 - Google Patents

通过低温蒸馏分离空气的方法和装置 Download PDF

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CN105637311B
CN105637311B CN201480056481.6A CN201480056481A CN105637311B CN 105637311 B CN105637311 B CN 105637311B CN 201480056481 A CN201480056481 A CN 201480056481A CN 105637311 B CN105637311 B CN 105637311B
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B·达维迪安
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

本发明涉及一种在包括在第一压力下运行的第一塔(21)、在低于第一压力的第二压力下运行的第二塔(23)和在低于第二压力的第三压力下运行的第三塔(25)的一组塔中通过低温蒸馏分离空气的方法，其中第三塔包括第一和第二蒸发器‑冷凝器(29,31)并将来自冷压缩机(47)的氮气送往蒸发器‑冷凝器之一。

Description

通过低温蒸馏分离空气的方法和装置
本发明涉及通过低温蒸馏分离空气的方法和单元。
在向气化工艺供氧的领域内，加压(通常50bara和更高)的不纯氧气(通常大约95摩尔％)的消耗伴随着用于气化器和用于相关燃气轮机的加压氮气的消耗。
当客户将所有可得的加压氮气再循环时，具有加压的低压塔的布置能够获得良好的氧气分离能量。低压塔当在大于2bar abs的压力下运行时被说成是“加压的”。
提出通过塔之间的更充分热集成改进此类系统的效率。
在天然具有交换线路的不同热端的布置中或如果有制冷能力要再循环，本发明特别有利。
会用到本发明的工艺的典型热端温差为6至10℃。
US-A-5341646描述了包含三个塔的分离单元——高压塔、低压塔和在低压与高压之间的压力下运行的中压塔。
将空气送往高压塔并且来自高压塔顶部的氮气在中压塔的中间冷凝器中冷凝。循环氮气料流在中压塔的底部冷凝器中冷凝。在中压塔的顶部产生气态氮。
来自中压塔顶部的氮气在低压塔的底部冷凝并将来自低压塔的液态氧加压并在交换线路中汽化。
US-A-6286336和US-A-5675977描述了最接近本发明的现有技术。
根据本发明的一个主题，提供一种在包含在第一压力下运行的第一塔、在低于第一压力的第二压力下运行的第二塔和在低于第二压力的第三压力下运行的第三塔的一组塔中通过低温蒸馏分离空气的方法，其中：
i)将压缩、净化并冷却的空气送往第一塔，在此将其分离以形成富氧液体和富氮气体，
ii)将一部分来自第一塔的富氮气体在第二塔的底部汽化器-冷凝器中冷凝，
iii)将富氧液体从第一塔送往第二塔，
iv)将富氧液体从第二塔的底部送往第三塔，
v)将富氮气体从第二塔的顶部送往第三塔的第一汽化器-冷凝器，在此将其冷凝，将冷凝液送回第二塔，
vi)从第三塔的顶部取出高氮气体(nitrogen-rich gas)，
vii)从第三塔的底部取出含有至少85％氧的液体，加压并汽化以形成含有至少85％氧的气态产物，
其特征在于第三塔的第一汽化器-冷凝器是位于第三塔的中间点的汽化器-冷凝器，第三塔具有作为底部汽化器-冷凝器的第二汽化器-冷凝器，来自第二塔的富氮气体在入口温度低于环境温度的压缩机中压缩并送往第二汽化器-冷凝器以在其中冷凝，第二塔的汽化器-冷凝器是作为第二塔中存在的唯一汽化器-冷凝器的底部汽化器-冷凝器，来自第一塔的塔顶气体在未经压缩的情况下送往第二塔的汽化器-冷凝器，任选将高氮液体(nitrogen-rich liquid)加压，然后从第二塔的顶部送往第一塔的顶部，从第一塔的顶部取出气态氮并再加热以形成工艺产物。
根据其它任选特征：
-将中间液体从第一塔送往第三塔；
-将来自第二塔的顶部的所有富氮气体送往第一和第二汽化器-冷凝器；
-在汽化或伪汽化前将所述含有至少85％氧的液体加压到高于30bar abs，优选高于40bara的压力；
-第三压力高于2bar abs；
-入口温度低于环境温度的所述压缩机的入口温度高于所述含有至少85％氧的液体的汽化温度减5℃；
-所述含有至少85％氧的液体在热交换器中汽化，在此将压缩空气冷却，所述热交换器的热端温差小于10℃，优选小于6℃。
根据本发明的另一主题，提供一种通过低温蒸馏分离空气的单元，其包含一组塔，该组塔包括在第一压力下运行的第一塔、在低于第一压力的第二压力下运行的第二塔和在低于第二压力的第三压力下运行的第三塔，第二塔具有底部汽化器-冷凝器，第三塔具有第一汽化器-冷凝器；用于将压缩、净化并冷却的空气送往第一塔的管线，在第一塔将其分离以形成富氧液体和富氮气体；用于将一部分来自第一塔的富氮气体送往在第二塔的底部汽化器-冷凝器中冷凝的管线；用于将富氧液体从第一塔送往第二塔的管线；用于将富氧液体从第二塔的底部送往第三塔的管线；用于将富氮气体从第二塔的顶部送往在此将其冷凝的第三塔的第一汽化器-冷凝器的管线；用于将冷凝液从第一汽化器-冷凝器送往第二塔的管线；用于从第三塔的顶部取出高氮气体(nitrogen-rich gas)的管线；用于从第三塔的底部取出含有至少85％氧的液体的管线；用于将所述液体加压的装置和用于汽化所述加压液体以形成含有至少85％氧的气态产物的热交换器，其特征在于第三塔的第一汽化器-冷凝器是位于第三塔的中间点的汽化器-冷凝器，第三塔具有作为底部汽化器-冷凝器的第二汽化器-冷凝器，来自第二塔的富氮气体在入口温度低于环境温度的压缩机中压缩并送往第二汽化器-冷凝器以在其中冷凝，第二塔的汽化器-冷凝器是作为第二塔中存在的唯一汽化器-冷凝器的底部汽化器-冷凝器，所述单元包含用于将来自第一塔的塔顶气体在未经压缩的情况下送往第二塔的汽化器-冷凝器的装置、任选的用于将高氮液体(nitrogen-richliquid)加压的装置和用于将所述加压高氮液体从第二塔的顶部送往第一塔的顶部的装置，和用于从第一塔的顶部取出富氮气体的管线和用于将其再加热以形成工艺产物的装置。
该单元可包含用于将中间液体从第一塔送往第三塔的装置。
该单元可包含用于将来自第二塔的顶部的所有富氮气体送往第一和第二汽化器-冷凝器的装置。
冷压缩机的使用能够通过级联效应极大降低第一塔的压力，以实现显著节能。
参考附图更详细描述本发明。
气体分离单元包含热交换器13、热交换器49、在11至20bara的第一压力下运行的第一塔21、在低于第一压力并在1至11bara之间的第二压力下运行的第二塔23和在低于第二压力的第三压力下运行的第三塔25。第三压力为2bar abs至6bara。
将空气1压缩至第一压力，然后一分为二。在第一压力下的一部分5在热交换器13中冷却并以气体形式送往第一塔21。剩余部分3在增压器7中增压至49bara的压力并一分为二。将一部分15送往热交换器13，在此将其冷却至该热交换器的中间温度，然后在Claude涡轮机11中膨胀并在与料流5混合后送往塔21以形成料流14。增压空气的剩余部分17再在耦合到涡轮机11上的增压器9中增压并送往热交换器13，在此将其冷却。冷却并伪液化的(pseudo-liquefied)料流17在涡轮机19中膨胀以形成至少部分液态料流，将其送往塔21。将所有空气1送往塔21，在此将其分离。
富氧料流33在膨胀后从第一塔送往第二塔23的中部。中间料流35在49中过冷(subcooling)然后膨胀后从第一塔送往第三塔25。将来自第一塔21的顶部的液氮过冷，然后膨胀，并在49中过冷然后膨胀后送往第三塔25的顶部。从第一塔中取出气态氮65并在热交换器13中再加热以形成氮气产物，将其加压为11至20bara。
另一部分氮气在第二塔的底部汽化器-冷凝器27中冷凝并送回第一塔的顶部。
将来自第二塔23的塔底液体51过冷，然后膨胀并送往第三塔25的中间高度。将来自第二塔23的塔顶液体39一分为二，将一部分55过冷，然后膨胀并送往第三塔25的顶部，其余部分53用泵57加压以送回第一塔21的顶部。将来自第二塔23的塔顶气体41一分为二。将一部分43送往位于第三塔25的中间高度的第一汽化器-冷凝器31。一部分43在其中冷凝并送往第二塔23的顶部。将气体41的另一部分45送回热交换器13，在此将其再加热到-120℃的温度。将该部分45再加热到比液体59的汽化温度减5℃高的温度。在这一实例中，该部分45位于低于加压氧气的汽化平台不超过5℃的温度水平。该部分45也可位于这一平台以上的温度水平。接着，将气体45在压缩机47中压缩，送回热交换器13，在此将其冷却到冷端，并送往第二汽化器-冷凝器29，其是第三塔25的底部汽化器-冷凝器。该部分45在汽化器-冷凝器29中冷凝并将冷凝料流膨胀和送往第二塔23的顶部。
从第三塔25的顶部取出塔顶气体63并在热交换器49,13中再加热以充当废气。来自第三塔25的塔底液体59含有至少85摩尔％氧，或甚至至少95摩尔％氧，但少于98％氧。这种液体59用泵61加压到至少30bar abs的压力，然后在热交换器13中汽化(或如果其压力超临界，则为伪汽化)以形成要送往气化器的加压氧气料流。
热交换器13的热端温差小于10℃，优选小于6℃，例如2℃至3℃。

Claims (16)

1.一种通过低温蒸馏分离空气的方法，所述方法在一组塔中进行，该组塔包括在第一压力下运行的第一塔(21)、在低于第一压力的第二压力下运行的第二塔(23)和在低于第二压力的第三压力下运行的第三塔(25)，其中：
i)将压缩、净化并冷却的空气送往第一塔，在此将其分离以形成富氧液体和富氮气体，
ii)将一部分来自第一塔的富氮气体在第二塔的底部汽化器-冷凝器(27)中冷凝，
iii)将富氧液体(33)从第一塔送往第二塔，
iv)将富氧液体从第二塔的底部送往第三塔，
v)将富氮气体(43)从第二塔的顶部送往第三塔的第一汽化器-冷凝器(31)，在此将其冷凝，将冷凝液送回第二塔，
vi)从第三塔的顶部取出高氮气体(63)，
vii)从第三塔的底部取出含有至少85％氧的液体(59)，加压并汽化以形成含有至少85％氧的气态产物，
其特征在于第三塔的第一汽化器-冷凝器是位于第三塔的中间点的汽化器-冷凝器，第三塔具有作为底部汽化器-冷凝器的第二汽化器-冷凝器(29)，来自第二塔的富氮气体在入口温度低于环境温度的压缩机(47)中压缩并送往第二汽化器-冷凝器以在其中冷凝，第二塔的汽化器-冷凝器(27)是作为第二塔中存在的唯一汽化器-冷凝器的底部汽化器-冷凝器，来自第一塔的塔顶气体在未经压缩的情况下送往第二塔的汽化器-冷凝器，任选将高氮液体加压，然后从第二塔的顶部送往第一塔的顶部，从第一塔的顶部取出气态氮并再加热以形成工艺产物。
2.如权利要求1中所述的方法，其中将中间液体(35)从第一塔(21)送往第三塔(25)。
3.如权利要求1中所述的方法，其中将来自第二塔的顶部的所有富氮气体送往第一汽化器-冷凝器(31)和第二汽化器-冷凝器(29)。
4.如权利要求1中所述的方法，其中在汽化或伪汽化前将所述含有至少85％氧的液体(59)加压到高于30bar abs的压力。
5.如权利要求1中所述的方法，其中在汽化或伪汽化前将所述含有至少85％氧的液体(59)加压到高于40bar abs的压力。
6.如权利要求1中所述的方法，其中第三压力高于2bar abs。
7.如权利要求1中所述的方法，其中入口温度低于环境温度的所述压缩机(47)的入口温度高于所述含有至少85％氧的液体的汽化温度减5℃。
8.如权利要求1中所述的方法，其中所述含有至少85％氧的液体在热交换器(13)中汽化，在此将压缩空气冷却，所述热交换器的热端温差小于10℃。
9.如权利要求1中所述的方法，其中所述含有至少85％氧的液体在热交换器(13)中汽化，在此将压缩空气冷却，所述热交换器的热端温差小于6℃。
10.一种通过低温蒸馏分离空气的单元，其包含一组塔，该组塔包括在第一压力下运行的第一塔(21)、在低于第一压力的第二压力下运行的第二塔(23)和在低于第二压力的第三压力下运行的第三塔(25)，第二塔具有底部汽化器-冷凝器(27)，第三塔具有第一汽化器-冷凝器(31)；用于将压缩、净化并冷却的空气送往第一塔的管线，在此将其分离以形成富氧液体和富氮气体；用于将一部分来自第一塔的富氮气体送往在第二塔的底部汽化器-冷凝器中冷凝的管线；用于将富氧液体(33)从第一塔送往第二塔的管线；用于将富氧液体从第二塔的底部送往第三塔的管线；用于将富氮气体(43)从第二塔的顶部送往在此将其冷凝的第三塔的第一汽化器-冷凝器的管线；用于将冷凝液从第一汽化器-冷凝器送往第二塔的管线；用于从第三塔的顶部取出高氮气体(63)的管线；用于从第三塔的底部取出含有至少85％氧的液体(59)的管线；用于将所述液体加压的装置(61)和用于汽化所述加压液体以形成含有至少85％氧的气态产物的热交换器，其特征在于第三塔的第一汽化器-冷凝器是位于第三塔的中间点的汽化器-冷凝器，第三塔具有作为底部汽化器-冷凝器的第二汽化器-冷凝器(29)，来自第二塔的富氮气体在入口温度低于环境温度的压缩机(47)中压缩并送往第二汽化器-冷凝器以在其中冷凝，第二塔的汽化器-冷凝器是作为第二塔中存在的唯一汽化器-冷凝器的底部汽化器-冷凝器，所述单元包含用于将来自第一塔的塔顶气体在未经压缩的情况下送往第二塔的汽化器-冷凝器的装置、任选的用于将高氮液体加压的装置和用于将所述加压高氮液体从第二塔的顶部送往第一塔的顶部的装置，和用于从第一塔的顶部取出富氮气体的管线和用于将其再加热以形成工艺产物的装置。
11.如权利要求10中所述的单元，其包含用于将中间液体(35)从第一塔送往第三塔的装置。
12.如权利要求10中所述的单元，其包含用于将来自第二塔的顶部的所有富氮气体送往第一汽化器-冷凝器(31)和第二汽化器-冷凝器(29)的装置。
13.如权利要求11中所述的单元，其包含用于将来自第二塔的顶部的所有富氮气体送往第一汽化器-冷凝器(31)和第二汽化器-冷凝器(29)的装置。
14.如权利要求10至13之一中所述的单元，其包含用于在汽化或伪汽化前将所述含有至少85％氧的液体加压到高于30bar abs的压力的装置。
15.如权利要求10至13之一中所述的单元，其包含用于在汽化或伪汽化前将所述含有至少85％氧的液体加压到高于40bar abs的压力的装置。
16.如权利要求10至13之一中所述的单元，其包含热交换器、用于将压缩空气送往其中以冷却的装置和用于将所述含有至少85％氧的液体送往其中以汽化的装置。
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