CN108332510A - 一种提高HyCO冷箱CO回收率的系统及方法 - Google Patents

一种提高HyCO冷箱CO回收率的系统及方法 Download PDF

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CN108332510A
CN108332510A CN201810241238.1A CN201810241238A CN108332510A CN 108332510 A CN108332510 A CN 108332510A CN 201810241238 A CN201810241238 A CN 201810241238A CN 108332510 A CN108332510 A CN 108332510A
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liquid
pipelines
low pressure
knockout
tanks
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徐晶
李现民
苏科峰
陆连根
钱海玲
宋孝林
谢惠云
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Shanghai Hualin Industrial Gas Co Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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Abstract

本发明涉及提高HyCO冷箱CO回收率的系统及方法。本发明在CO/CH4再沸器与CO/CH4分离塔塔顶之间的管线上外接补充管线，在补充管线上设置有液态CO罐，液态CO罐进口设置液态CO罐进口阀门，液态CO罐出口设置液态CO汽化器与液态CO汽化器出口阀门，该补充管线汇流至CO产品管线。由于增加一个液态CO罐、液态CO调节阀、液态CO汽化器来控制液态CO气化成气态CO产品。在正常运行中，遇到客户降低CO的使用量，H2使用量则不变。关小CO产品外送阀门，开大液态CO罐进口阀门，关小液态CO汽化器出口阀门，将液态CO罐液位提高。直到客户恢复CO产品的用量，将CO产品外送阀门开大，关小液态CO罐进口阀门开度，同时将液态CO汽化器出口阀门开大，降低液CO罐的液位。

Description

一种提高HyCO冷箱CO回收率的系统及方法
技术领域
本发明涉及一种HyCO冷箱系统，尤其是涉及一种提高HyCO冷箱CO回收率的系统及方法。
背景技术
目前，HYCO装置主要是将原料(合成气，成分包括54％左右的CO，45％左右的H2以及微量的N2、CH4，Ar)通过高压CO变为低压CO节流膨胀制冷，进入冷箱液化，利用各气体沸点不同，逐步脱除CH4，N2，Ar，并能够让CO和H2通过。提纯以后最终产品为H2和CO产品送给客户。
HYCO天然气蒸汽转化炉制H2装置，是通过天然气为原料和蒸汽反应制H2产品的装置。
同样100Nm3合成气进入冷箱，出来的CO产品为54Nm3，H2产品为45Nm3。客户会将CO和H2产品的使用比例控制在54％和45％，但是当下游客户装置发生不正常工况时，有部分的CO或者H2会多余出来，从而使得CO或者H2放空，通过长明灯燃烧。这就造成了资源的浪费，另外气态CO燃烧以后会产生温室效应。
有关文献提出可以利用CO总管其他客户来调节CO和H2的比例，但是对于HYCO冷箱来说只有单一的客户，调节CO放空的措施，显然是不合适的。虽然HYCO冷箱的H2是可以通过HYCO天然气蒸汽转化炉制H2来调整的。但是还需要额外设置天然气蒸汽转化炉，设备成本高，技术难度大。
发明内容
本发明的目的就是为了克服上述现有技术存在的缺陷而提供一种提高HyCO冷箱CO回收率的系统及方法。
本发明的目的可以通过以下技术方案来实现：
一种提高HyCO冷箱CO回收率的系统，包括：汽液分离罐、CO/CH4再沸器、N2/CO再沸器、N2/CO冷凝器、N2/CO分离塔、CO/CH4分离塔、H2汽提塔、液态CO罐、液态CO汽化器、CO压缩机、膨胀机、板翅换热器，汽液分离罐、H2汽提塔、N2/CO分离塔、CO/CH4分离塔顺序相连，板翅换热器设置在汽液分离罐前，CO/CH4再沸器与CO/CH4分离塔相连，N2/CO再沸器、N2/CO冷凝器分别与N2/CO分离塔相连，汽液分离罐前连接合成气原料管线，CO/CH4分离塔出口连接低压CO管线，低压CO管线与CO压缩机连接，CO压缩机后接CO产品管线与高压CO管线，所述膨胀机进口与高压CO管线连接，出口与低低压CO管线连接，
CO/CH4再沸器与CO/CH4分离塔塔顶之间的管线上外接补充管线，在补充管线上设置有液态CO罐，液态CO罐进口设置液态CO罐进口阀门，液态CO罐出口设置液态CO汽化器与液态CO汽化器出口阀门，该补充管线汇流至CO产品管线，CO产品管线上设置有CO产品外送阀门。
其中，N2/CO分离塔与N2/CO再沸器连接成循环回路，N2/CO分离塔与N2/CO冷凝器连接成循环回路。
其中，N2/CO分离塔与CO/CH4分离塔之间有两个连接管路，其中一个连接管路直接将N2/CO分离塔与CO/CH4分离塔连接，另一个连接管路经过板翅换热器。
其中，CO/CH4分离塔出口连接低压CO管线，低压CO管线与CO压缩机连接，CO压缩机后接CO产品管线与高压CO管线。
其中，高压CO管线分流成两部分，其中一部分通过板翅换热器后与膨胀机连接，膨胀机出口连接低低压CO管线，另一部分通过板翅换热器后，分成两股，一股与CO/CH4再沸器及CO/CH4分离塔连接，另一股经过N2/CO再沸器后汇流至低低压CO管线。
一种提高HyCO冷箱CO回收率的方法，包括以下步骤：
合成气原料管线先通过两个板翅换热器后，进入汽液分离罐，从汽液分离罐出来后进入H2汽提塔，H2汽提塔将H2分离处理，然后混合气进入N2/CO分离塔，
从N2/CO分离塔出来的第一部分物料经N2/CO再沸器再回流至N2/CO分离塔，第二部分物料经N2/CO冷凝器再回流至N2/CO分离塔，第三部分物料经板翅换热器换热后进入CO/CH4分离塔，第三部分物料的其中一部分经板翅换热器换热后进入CO/CH4分离塔，剩余部分直接进入CO/CH4分离塔，
从CO/CH4分离塔出来的物料为低压CO，低压CO经低压CO管线通过一个CO压缩机压缩后经CO产品管线排出，CO产品管线上设置有CO产品外送阀门，
低压CO经低压CO管线通过两个CO压缩机压缩后为高压CO，一部分高压CO经高压CO管线通过板翅换热器换热后，通过膨胀机膨胀后变为低低压CO，低低压CO经低低压CO管线通过CO压缩机压缩后可变为CO产品或高压CO，
另一部分高压CO经高压CO管线通过板翅换热器换热后，分成两股，一股经过CO/CH4再沸器后通过CO/CH4再沸器与CO/CH4分离塔塔顶之间的管线回流至CO/CH4分离塔，CO/CH4再沸器与CO/CH4分离塔塔顶之间的管线上外接补充管线，在补充管线上设置有液态CO罐，液态CO罐进口设置液态CO罐进口阀门，液态CO罐出口设置液态CO汽化器与液态CO汽化器出口阀门，该补充管线汇流至CO产品管线，
另一股经过N2/CO再沸器后汇流至低低压CO管线。
本发明在CO/CH4再沸器与CO/CH4分离塔塔顶之间的管线上外接补充管线。在补充管线上设置有液态CO罐，液态CO罐进口设置液态CO罐进口阀门，液态CO罐出口设置液态CO汽化器与液态CO汽化器出口阀门，该补充管线汇流至CO产品管线。由于增加一个液态CO罐、液态CO调节阀、液态CO汽化器来控制液态CO气化成气态CO产品。
在正常运行中，遇到客户降低CO的使用量，H2使用量则不变。关小CO产品外送阀门，开大液态CO罐进口阀门，关小液态CO汽化器出口阀门，将液态CO罐液位提高。直到客户恢复CO产品的用量，将CO产品外送阀门开大，关小液态CO罐进口阀门开度，同时将液态CO汽化器出口阀门开大，降低液CO罐的液位。
与现有技术相比，本发明具有以下优点及有益效果：
(1)本方法降低减少CO直接燃烧排放大气，减少温室气体排放。
(2)本方法增加了装置的利润。
(3)本方法增加了装置的稳定性。
附图说明
图1为实施例1中提高HyCO冷箱CO回收率的系统的结构示意图。
图中标号所示：1为CO产品外送阀门，2为CO压缩机，3为膨胀机，4为板翅换热器，5为高压CO管线，6为汽液分离罐，7为CO/CH4再沸器，8为N2/CO再沸器，9为N2/CO冷凝器，10为N2/CO分离塔，11为CO/CH4分离塔，12为H2汽提塔，13为液态CO罐进口阀门，14为液态CO罐，15为液态CO汽化器，16为液态CO汽化器出口阀门，17为合成气原料管线，18为低压CO管线，19为低低压CO管线，20为CO产品管线，21为补充管线。
具体实施方式
下面结合附图和具体实施例对本发明进行详细说明。
实施例
一种提高HyCO冷箱CO回收率的系统，如图1所示，包括：汽液分离罐6、CO/CH4再沸器7、N2/CO再沸器8、N2/CO冷凝器9、N2/CO分离塔10、CO/CH4分离塔11、H2汽提塔12、液态CO罐14、液态CO汽化器15、CO压缩机2、膨胀机3、板翅换热器4，汽液分离罐6、H2汽提塔12、N2/CO分离塔10、CO/CH4分离塔11顺序相连，板翅换热器4设置在汽液分离罐6前，CO/CH4再沸器7与CO/CH4分离塔11相连，N2/CO再沸器8、N2/CO冷凝器9分别与N2/CO分离塔10相连，汽液分离罐6前连接合成气原料管线17，CO/CH4分离塔11出口连接低压CO管线18，低压CO管线18与CO压缩机2连接，CO压缩机2后接CO产品管线20与高压CO管线5，膨胀机3进口与高压CO管线5连接，出口与低低压CO管线19连接，
CO/CH4再沸器7与CO/CH4分离塔11塔顶之间的管线上外接补充管线21，在补充管线21上设置有液态CO罐14，液态CO罐14进口设置液态CO罐进口阀门13，液态CO罐14出口设置液态CO汽化器15与液态CO汽化器出口阀门16，该补充管线21汇流至CO产品管线20，CO产品管线20上设置有CO产品外送阀门1。
其中，N2/CO分离塔10与N2/CO再沸器8连接成循环回路，N2/CO分离塔10与N2/CO冷凝器9连接成循环回路。
其中，N2/CO分离塔10与CO/CH4分离塔11之间有两个连接管路，其中一个连接管路直接将N2/CO分离塔10与CO/CH4分离塔11连接，另一个连接管路经过板翅换热器4。
其中，CO/CH4分离塔11出口连接低压CO管线18，低压CO管线18与CO压缩机2连接，CO压缩机2后接CO产品管线20与高压CO管线5。
其中，高压CO管线5分流成两部分，其中一部分通过板翅换热器4后与膨胀机3连接，膨胀机3出口连接低低压CO管线19，另一部分通过板翅换热器4后，分成两股，一股与CO/CH4再沸器7及CO/CH4分离塔11连接，另一股经过N2/CO再沸器8后汇流至低低压CO管线19。
一种提高HyCO冷箱CO回收率的方法，包括以下步骤：
合成气原料管线17先通过两个板翅换热器4后，进入汽液分离罐6，从汽液分离罐6出来后进入H2汽提塔12，H2汽提塔12将H2分离处理，然后混合气进入N2/CO分离塔10，
从N2/CO分离塔10出来的第一部分物料经N2/CO再沸器8再回流至N2/CO分离塔10，第二部分物料经N2/CO冷凝器9再回流至N2/CO分离塔10，第三部分物料经板翅换热器4换热后进入CO/CH4分离塔11，第三部分物料的其中一部分经板翅换热器4换热后进入CO/CH4分离塔11，剩余部分直接进入CO/CH4分离塔11，
从CO/CH4分离塔11出来的物料为低压CO，低压CO经低压CO管线18通过一个CO压缩机2压缩后经CO产品管线20排出，CO产品管线20上设置有CO产品外送阀门1，
低压CO经低压CO管线18通过两个CO压缩机2压缩后为高压CO，一部分高压CO经高压CO管线5通过板翅换热器4换热后，通过膨胀机3膨胀后变为低低压CO，低低压CO经低低压CO管线19通过CO压缩机2压缩后可变为CO产品或高压CO，
另一部分高压CO经高压CO管线5通过板翅换热器4换热后，分成两股，一股经过CO/CH4再沸器7后通过CO/CH4再沸器7与CO/CH4分离塔11塔顶之间的管线回流至CO/CH4分离塔11，CO/CH4再沸器7与CO/CH4分离塔11塔顶之间的管线上外接补充管线21，在补充管线21上设置有液态CO罐14，液态CO罐14进口设置液态CO罐进口阀门13，液态CO罐14出口设置液态CO汽化器15与液态CO汽化器出口阀门16，该补充管线21汇流至CO产品管线20，
另一股经过N2/CO再沸器8后汇流至低低压CO管线19。
本发明在CO/CH4再沸器7与CO/CH4分离塔11塔顶之间的管线上外接补充管线21。在补充管线21上设置有液态CO罐14，液态CO罐14进口设置液态CO罐进口阀门13，液态CO罐14出口设置液态CO汽化器15与液态CO汽化器出口阀门16，该补充管线21汇流至CO产品管线20。由于增加一个液态CO罐、液态CO调节阀、液态CO汽化器15来控制液态CO气化成气态CO产品。
在正常运行中，遇到客户降低CO的使用量，H2使用量则不变。关小CO产品外送阀门1，开大液态CO罐进口阀门13，关小液态CO汽化器出口阀门16，将液态CO罐14液位提高。直到客户恢复CO产品的用量，将CO产品外送阀门1开大，关小液态CO罐进口阀门13开度，同时将液态CO汽化器出口阀门16开大，降低液CO罐的液位。
上述的对实施例的描述是为便于该技术领域的普通技术人员能理解和使用发明。熟悉本领域技术的人员显然可以容易地对这些实施例做出各种修改，并把在此说明的一般原理应用到其他实施例中而不必经过创造性的劳动。因此，本发明不限于上述实施例，本领域技术人员根据本发明的揭示，不脱离本发明范畴所做出的改进和修改都应该在本发明的保护范围之内。

Claims (6)

1.一种提高HyCO冷箱CO回收率的系统，其特征在于，包括：汽液分离罐(6)、CO/CH4再沸器(7)、N2/CO再沸器(8)、N2/CO冷凝器(9)、N2/CO分离塔(10)、CO/CH4分离塔(11)、H2汽提塔(12)、液态CO罐(14)、液态CO汽化器(15)、CO压缩机(2)、膨胀机(3)、板翅换热器(4)，汽液分离罐(6)、H2汽提塔(12)、N2/CO分离塔(10)、CO/CH4分离塔(11)顺序相连，板翅换热器(4)设置在汽液分离罐(6)前，CO/CH4再沸器(7)与CO/CH4分离塔(11)相连，N2/CO再沸器(8)、N2/CO冷凝器(9)分别与N2/CO分离塔(10)相连，汽液分离罐(6)前连接合成气原料管线(17)，CO/CH4分离塔(11)出口连接低压CO管线(18)，低压CO管线(18)与CO压缩机(2)连接，CO压缩机(2)后接CO产品管线(20)与高压CO管线(5)，所述膨胀机(3)进口与高压CO管线(5)连接，出口与低低压CO管线(19)连接，
CO/CH4再沸器(7)与CO/CH4分离塔(11)塔顶之间的管线上外接补充管线(21)，在补充管线(21)上设置有液态CO罐(14)，液态CO罐(14)进口设置液态CO罐进口阀门(13)，液态CO罐(14)出口设置液态CO汽化器(15)与液态CO汽化器出口阀门(16)，该补充管线(21)汇流至CO产品管线(20)，CO产品管线(20)上设置有CO产品外送阀门(1)。
2.根据权利要求1所述的一种提高HyCO冷箱CO回收率的系统，其特征在于，N2/CO分离塔(10)与N2/CO再沸器(8)连接成循环回路，N2/CO分离塔(10)与N2/CO冷凝器(9)连接成循环回路。
3.根据权利要求2所述的一种提高HyCO冷箱CO回收率的系统，其特征在于，N2/CO分离塔(10)与CO/CH4分离塔(11)之间有两个连接管路，其中一个连接管路直接将N2/CO分离塔(10)与CO/CH4分离塔(11)连接，另一个连接管路经过板翅换热器(4)。
4.根据权利要求1所述的一种提高HyCO冷箱CO回收率的系统，其特征在于，CO/CH4分离塔(11)出口连接低压CO管线(18)，低压CO管线(18)与CO压缩机(2)连接，CO压缩机(2)后接CO产品管线(20)与高压CO管线(5)。
5.根据权利要求1所述的一种提高HyCO冷箱CO回收率的系统，其特征在于，高压CO管线(5)分流成两部分，其中一部分通过板翅换热器(4)后与膨胀机(3)连接，膨胀机(3)出口连接低低压CO管线(19)，
另一部分通过板翅换热器(4)后，分成两股，一股与CO/CH4再沸器(7)及CO/CH4分离塔(11)连接，另一股经过N2/CO再沸器(8)后汇流至低低压CO管线(19)。
6.一种提高HyCO冷箱CO回收率的方法，其特征在于，包括以下步骤：
合成气原料管线(17)先通过两个板翅换热器(4)后，进入汽液分离罐(6)，从汽液分离罐(6)出来后进入H2汽提塔(12)，H2汽提塔(12)将H2分离处理，然后混合气进入N2/CO分离塔(10)，
从N2/CO分离塔(10)出来的第一部分物料经N2/CO再沸器(8)再回流至N2/CO分离塔(10)，第二部分物料经N2/CO冷凝器(9)再回流至N2/CO分离塔(10)，第三部分物料经板翅换热器(4)换热后进入CO/CH4分离塔(11)，第三部分物料的其中一部分经板翅换热器(4)换热后进入CO/CH4分离塔(11)，剩余部分直接进入CO/CH4分离塔(11)，
从CO/CH4分离塔(11)出来的物料为低压CO，低压CO经低压CO管线(18)通过一个CO压缩机(2)压缩后经CO产品管线(20)排出，CO产品管线(20)上设置有CO产品外送阀门(1)，
低压CO经低压CO管线(18)通过两个CO压缩机(2)压缩后为高压CO，一部分高压CO经高压CO管线(5)通过板翅换热器(4)换热后，通过膨胀机(3)膨胀后变为低低压CO，低低压CO经低低压CO管线(19)通过CO压缩机(2)压缩后可变为CO产品或高压CO，
另一部分高压CO经高压CO管线(5)通过板翅换热器(4)换热后，分成两股，一股经过CO/CH4再沸器(7)后通过CO/CH4再沸器(7)与CO/CH4分离塔(11)塔顶之间的管线回流至CO/CH4分离塔(11)，CO/CH4再沸器(7)与CO/CH4分离塔(11)塔顶之间的管线上外接补充管线(21)，在补充管线(21)上设置有液态CO罐(14)，液态CO罐(14)进口设置液态CO罐进口阀门(13)，液态CO罐(14)出口设置液态CO汽化器(15)与液态CO汽化器出口阀门(16)，该补充管线(21)汇流至CO产品管线(20)，
另一股经过N2/CO再沸器(8)后汇流至低低压CO管线(19)。
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