CN107490244A - 一种低功耗co深冷分离系统及其分离方法 - Google Patents

一种低功耗co深冷分离系统及其分离方法 Download PDF

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CN107490244A
CN107490244A CN201710625038.1A CN201710625038A CN107490244A CN 107490244 A CN107490244 A CN 107490244A CN 201710625038 A CN201710625038 A CN 201710625038A CN 107490244 A CN107490244 A CN 107490244A
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曹卫华
文向南
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CHENGDU SHENLENG LIQUEFACTION PLANT Co Ltd
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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Abstract

本发明公开了一种低功耗CO深冷分离系统，包括脱碳气净化单元、深冷分离单元、PSA制氢单元、解析气压缩机单元和循环压缩机单元，还公开了一种低功耗CO深冷分离系统的分离方法，具有脱碳气净化、冷凝分离脱氢、精馏塔、循环压缩机、PSA制氢和解析气压缩机的工艺步骤。本发明的有益效果是：采用富氢尾气或净化气做再生气，确保PSA制氢单元的解析气不含水和CO2；通过单独设置解析气换热通道和低温分离器，大幅降低解析气压缩机的功耗；采用氮气循环压缩机代替效率较低的CO循环压缩机，降低循环压缩机的功耗，还能够缩短装置的启动时间、减少启动阶段的放空量；能耗低、启动快、投资省、排放少，具有良好的经济效益和环保效益。

Description

一种低功耗CO深冷分离系统及其分离方法
技术领域
本发明涉及一种低功耗CO深冷分离系统及其分离方法，属于深冷气体分离领域。
背景技术
CO是重要的羰基合成原料气，由CO出发可以制取几乎所有的有机化学品，但在生产乙二醇、醋酸和二甲基二酰胺等化工产品过程中对原料CO的纯度要求非常高(≥98.5％)。深冷分离技术工艺成熟，操作稳定、处理量大、产品纯度高、收率高，是目前CO分离的首选技术。
为提高经济效益，目前很多煤制甲醇或合成氨装置通过部分改造联产乙二醇，与新建乙二醇装置相比设备投资低、建设周期短。但鉴于煤制甲醇或合成氨装置的合成气压力远高于乙二醇装置所需的压力，若采用常规工艺，将导致CO深冷分离装置的能耗增加。
中国发明专利CN 1907849 B“从合成气获得产品的方法和装置”是一种典型的CO深冷分离工艺：PSA制氢的解析气经增压后返回原料气管线，同时采用CO压缩、制冷循环。该工艺的解析气压缩机和CO循环压缩机的功耗和投资较大，同时装置的启动时间长、启动阶段的放空量大。
本发明提出了一种低功耗CO深冷分离系统及其分离方法，比较实用、完美和方便地解决了上述问题。
发明内容
本发明的目的在于克服现有技术的缺点，提供一种能耗低、启动快、成本低的低功耗CO深冷分离系统及其分离方法。
本发明的目的通过以下技术方案来实现：一种低功耗CO深冷分离系统，包括脱碳气净化单元、深冷分离单元、PSA制氢单元、解析气压缩机单元和循环压缩机单元；
所述的脱碳气净化单元包括脱碳气流道A和再生气B，脱碳气流道A的入口连接在脱碳气储存器上，再生气流道B的出口经开关阀门后连接在富氢尾气储存器上；
所述的深冷分离单元包括板式换热器、净化气低温分离器、解析气低温分离器、低温闪蒸罐、精馏塔和塔顶冷凝器，板式换热器中设置有流道Ⅰ、流道Ⅱ、流道Ⅲ、流道Ⅳ、流道Ⅴ、流道Ⅵ、流道Ⅶ、流道Ⅷ和流道Ⅸ，脱碳气流道A出口与板式换热器的流道Ⅲ相连后连接在净化器低温分离气的中部入口上，净化气低温分离器顶部和底部分别设置有顶部出口和底部出口，净化器低温分离器顶部出口与板式换热器的流道Ⅳ相连后连接在再生气流道B的入口上，净化气低温分离器底部出口经减压阀门V1后连接在低温闪蒸罐的中部入口上；
低温闪蒸罐上开有顶部出口和底部出口，低温闪蒸罐顶部出口经板式换热器流道Ⅱ后连接在闪蒸气储存器上，闪蒸气储存器入口处设置有开关阀门，低温闪蒸器底部出口经减压阀门V4后连接在精馏塔中部入口上，精馏塔上开有顶部出口、上部出口和底部出口，精馏塔顶部出口经板式换热器流道Ⅰ后连接在富氮尾气储存器上，在板式换热器流道Ⅰ和富氮尾气储存器相连的管道上设置有开关阀门，精馏塔底部出口经减压阀门V5后再与板式换热器流道Ⅶ入口相连，板式换热器流道Ⅶ出口连接在CO产品储存器上，精馏塔上部出口连接在塔顶冷凝器上；
塔顶冷凝器包括入口E、入口F、出口G和出口H，精馏塔上部出口连接在冷凝器入口F上，冷凝器的出口G连接在精馏塔上部的入口上；
还包括液氮储存器，液氮储存器经减压阀门V7后连接在冷凝器入口E上，冷凝器出口H经板式换热器流道Ⅷ后连接在循环压缩机单元入口上，循环压缩机单元的出口与板式换热器的流道Ⅸ入口相连，板式换热器流道Ⅸ出口通过管道连接在减压阀门V6和冷凝器入口E相连的管道上；
在净化气低温分离器的顶部出口和板式换热器流道Ⅳ相连的管道上开有分支管，该分支管经减压阀门V2后连接在板式换热器流道Ⅴ的入口上，板式换热器流道Ⅴ出口连接在PSA制氢单元的入口上，PSA制氢单元上开有出口C和出口D，PSA制氢单元出口C连接在氢气产品储存器上，PSA制氢单元出口D经解析气压缩机单元后连接在板式换热器流道Ⅵ进口上，板式换热器流道Ⅵ出口连接在解析气低温分离器中部入口上，解析气低温分离器开有顶部出口和底部出口，解析气低温分离器顶部出口通过管道连接在减压阀门V2和板式蒸发器流道Ⅴ入口相连的管道上，解析气低温分离器底部出口经减压阀门V3后连接在减压阀门V1和低温闪蒸器中部入口相连的管道上。
所述的低温闪蒸罐为一次分离型或蒸发汽提型。
所述的循环压缩机单元为离心式或活塞式压缩机。
所述的解析气压缩机单元为离心式或螺杆式压缩机。
所述的解析气压缩机单元和循环压缩机单元为电机驱动或汽轮机“一拖二”驱动。
一种低功耗CO深冷分离系统的分离方法，包括以下步骤：
S1、脱碳气储存器中装有脱碳气，脱碳气中含水、甲醇和CO2杂质，脱碳气进入脱碳气净化单元中被脱除水、甲醇和CO2杂质，变为净化气，净化气进入板式换热器流道III被冷却为气相净化气和液相净化气，气相净化气和液相净化气一起进入净化气低温分离器分离，分离后的液相净化气从净化气低温器的底部出口进入低温闪蒸罐中，分离后的气相净化气分为两股，一股返回至板式换热器流道Ⅳ复热至常温后进入脱碳气净化单元工作后，最终被富氢尾气储存器收集，另一股气相返回至板式换热器流道V复热至常温后进入PSA制氢单元中，作为PSA制氢单元的原料气，在PSA制氢单元作用下，原料气变为氢气产品和解析气，氢气产品经PSA制氢单元出口C流出后被氢气产品储存器收集，解析气经解析气压缩机压缩后再进入板式换热器流道Ⅵ被冷却，冷却后的解析气进入解析气低温分离器进行分离，分离后的气相解析气和净化气低温器顶部出口的部分净化气混合，一起进入板式换热器的流道V复热，分离后的液相解析气从解析气低温分离器的底部出口进入低温闪蒸罐中；
S2、液相净化气进入低温闪蒸罐中后进行第二次分离，分离后变为气相闪蒸气和液相闪蒸气，气相闪蒸气通过板式换热器流道II复热至常温后被闪蒸气储存器收集，液相闪蒸气被经减压阀门V4减压后送至精馏塔中部，经过精馏塔精馏，精馏塔精馏后得到富氮尾气和CO液体，富氮尾气分为两股，一股富氮尾气返回至板式换热器流道I复热至常温后被富氮尾气储存器收集，另一股富氮尾气通过入口F连接在塔顶冷凝器上，在其中被液氮冷凝后从出口G引出，回流至精馏塔(6)的上部入口，CO液体经减压阀门V5减压后返回至板式换热器流道VII复热至常温后被CO产品储存器收集；
S3、液氮储存器中的液氮通过减压阀门V7后经过入口E进入塔顶冷凝器，液氮在塔顶冷凝器中被部分气化，气化后的氮气经板式换热器流道VIII复热至常温后，再进入循环压缩机单元压缩变成中压氮气，该中压氮气经板式换热器流道Ⅸ、减压阀门V6后与液氮储存器流出的液氮相混合，混合后再一起进入塔顶冷凝器中实现循环；
所述的解析气压缩机单元的排气压力在2.5～4.0MPa.G之间。
所述的解析气压缩机和解析气低温分离器之间设置有板式换热器的流道VI，该流道VI为单独的解析气换热流道。
所述的循环压缩机单元的压缩介质为氮气，进口压力在0.05～0.5MPa.G之间，排气压力在0.6～3.5MPa.G之间。
本发明具有以下优点：
(1)采用富氢尾气或净化气做再生气，确保PSA制氢单元的解析气不含水和CO2；
(2)通过单独设置解析气换热通道和低温分离器，降低解析气压缩机的排压，从而大幅降低解析气压缩机的功耗和投资；
(3)采用氮气循环压缩机代替效率较低的CO循环压缩机，降低循环压缩机的功耗和投资，还可以缩短装置的启动时间、减少启动阶段的放空量；
(4)本发明能耗低、启动快、投资省、排放少，具有良好的经济效益和环保效益。
附图说明
图1为本发明的实施例一的结构示意图；
图2为本发明的实施例二的结构示意图；
图3为本发明的实施例三的结构示意图；
图4为本发明的实施例四的结构示意图；
图中，1-脱碳气净化单元，2-板式换热器，3-净化气低温分离器，4-解析气低温分离器，5-低温闪蒸罐，6-精馏塔，7-塔顶冷凝器，8-PSA制氢单元，9-解析气压缩机单元，10-循环压缩机单元，11-深冷分离单元。
具体实施方式
下面结合附图对本发明做进一步的描述，本发明的保护范围不局限于以下所述：
实施例一：如图1所示，一种低功耗CO深冷分离系统，它包括脱碳气净化单元、深冷分离单元、PSA制氢单元、解析气压缩机单元和循环压缩机单元；
在本实施例中，所述的脱碳气净化单元1包括脱碳气流道A和再生气流道B，脱碳气流道A的出口与板式换热器2流道III的入口相连，再生气流道B的入口与板式换热器2流道IV的出口相连；
在本实施例中，所述的深冷分离单元11包括板式换热器2、净化气低温分离器3、解析气低温分离器4、低温闪蒸罐5、精馏塔6和塔顶冷凝器7，板式换热器2流道III的出口与净化气低温分离器3的入口相连，净化气低温分离器3的液相出口经阀门V1减压后与低温闪蒸罐5的入口相连，净化气低温分离器3的气相出口分成两股：一股与板式换热器2流道IV的入口相连，另一股经阀门V2减压后与板式换热器2流道V的入口相连，板式换热器2流道VI的出口与解析气低温分离器4的入口相连，解析气低温分离器4的液相出口经阀门V3减压后与低温闪蒸罐5的入口相连，解析气低温分离器4的气相出口与板式换热器2流道V的入口相连，低温闪蒸罐5的液相出口经阀门V4减压后与精馏塔6的中部相连，低温闪蒸罐5的气相出口与板式换热器2流道II的入口相连，精馏塔6的液相出口经阀门V5减压后板式换热器2流道VII的入口相连，精馏塔6的气相出口分成两股：一股与板式换热器2流道I的入口相连，另一股与塔顶冷凝器7的入口F相连，板式换热器2流道IX的出口经阀门V6减压后与塔顶冷凝器7的入口E相连，塔顶冷凝器7的出口H与板式换热器2流道VIII的入口相连；
在本实施例中，所述的PSA制氢单元8的入口与板式换热器2流道V的出口相连，出口C为氢气产品，出口D与解析气压缩机单元9的入口相连；
在本实施例中，所述的解析气压缩机单元9的出口与板式换热器2流道VI的入口相连；
在本实施例中，所述的循环压缩机单元10的入口与板式换热器2流道VIII的出口相连，循环压缩机单元10的出口与板式换热器2流道IX的入口相连。
在本实施例中，所述的低温闪蒸罐5为一次分离型。
在本实施例中，所述的解析气压缩机单元9和循环压缩机单元10均为电机驱动且均为离心式压缩机。
一种低功耗CO深冷分离系统的分离方法，它包括以下步骤，
S1、脱碳气经脱碳气净化单元1脱除其中的杂质(水、甲醇和CO2)后，在板式换热器2的流道III中被冷流体冷却并部分冷凝，随后进入净化气低温分离器3中进行第一次分离，分离后的液相经阀门V1减压后送入低温闪蒸罐5进行第二次分离，分离后的气相分成两股：一股直接返回至板式换热器2的流道IV中复热至常温后作为脱碳气净化单元1的再生气；另一股经阀门V2减压后与解析气低温分离器4的气相混合，一起返回至板式换热器2流道V复热至常温，作为PSA制氢单元8的原料气；
S2、PSA制氢单元8的产品有两股：出口C为氢气产品，出口D为解析气，解析气经解析气压缩机单元9增压后，在板式换热器2的流道VI中被冷流体冷却并部分冷凝，随后进入解析气低温分离器4中进行第一次分离，分离后的液相经阀门V3减压后也送入低温闪蒸罐5进行第二次分离，分离后的气相返回至板式换热器2流道V复热至常温，作为PSA制氢单元8的原料气；
S3、经低温闪蒸罐5的第二次分离后，塔顶闪蒸气返回至板式换热器2流道II复热至常温，塔底液相经阀门V4减压后送入精馏塔6的中部，经过精馏塔6的进一步精馏，在塔顶得到的富氮尾气返回至板式换热器2流道I复热至常温，塔底得到的CO液体经阀门V5减压后返回至板式换热器2流道VII复热至常温；
S4、从循环压缩机单元10送来的增压氮气在板式换热器2的流道IX中被冷流体冷却、冷凝并过冷后，经阀门V6减压后与界区外的液氮混合，一起作为塔顶冷凝器7的冷源，在塔顶冷凝器7中被部分气化的低压液氮返回至板式换热器2流道VIII复热至常温后，进入循环压缩机单元10的入口再次压缩而循环制冷。
在本实施例中，原料气压力5.3MPa.G，解析气压缩机单元9的排气压力为3.3MPa.G；循环压缩机单元10的压缩介质为氮气，进口压力0.25MPa.G，排气压力1.6MPa.G。
在本实施例中，以年产20万吨合成气制乙二醇装置为例，与常规工艺相比，如下表所示，其能耗降幅达8.5％，年节约电费185.6万元。
实施例2：如图2所示，本实施例与实施例1的区别在于：低温闪蒸罐5采用蒸发汽提塔，从而适当提高CO和氢的回收率。
实施例3：如图3所示，本实施例与实施例1的区别在于：在脱碳气净化单元1脱碳气流道A的出口增加一股至再生气流道B入口的旁通管线及阀门V8，用于脱碳气净化单元1的启动或补充用再生气。
实施例4：如图4所示，本实施例与实施例1的区别在于：在解析气压缩机9上还设置有另外一个入口，板式换热器2流道II的出口直接与解析气压缩机单元9的级间相连，实现闪蒸气的回收，从而适当提高CO和氢的回收率。
最后应说明的是：以上各实施例仅用以说明本发明的技术方案，而非对其限制；尽管参照前述各实施例对本发明进行了详细的说明，本领域的普通技术人员应当理解：其依然可以对前述各实施例所记载的技术方案进行修改，或者对其中部分或者全部技术特征进行等同替换；而这些修改或者替换，并不使相应技术方案的本质脱离本发明各实施例技术方案的范围。

Claims (9)

1.一种低功耗CO深冷分离系统，其特征在于：包括脱碳气净化单元（1）、深冷分离单元（11）、PSA制氢单元（8）、解析气压缩机单元（9）和循环压缩机单元（10）；
所述的脱碳气净化单元（1）包括脱碳气流道A和再生气流道B，脱碳气A的入口连接在脱碳气储存器上，再生气流道B的出口经开关阀门后连接在富氢尾气储存器上；
所述的深冷分离单元（11）包括板式换热器（2）、净化气低温分离器（3）、解析气低温分离器（4）、低温闪蒸罐（5）、精馏塔（6）和塔顶冷凝器（7），板式换热器（2）中设置有流道Ⅰ、流道Ⅱ、流道Ⅲ、流道Ⅳ、流道Ⅴ、流道Ⅵ、流道Ⅶ、流道Ⅷ和流道Ⅸ，脱碳气流道A出口与板式换热器（2）的流道Ⅲ相连后连接在净化器低温分离气（3）的中部入口上，净化气低温分离器（3）顶部和底部分别设置有顶部出口和底部出口，净化器低温分离器顶部出口与板式换热器（2）的流道Ⅳ相连后连接在再生气流道B的入口上，净化气低温分离器（3）底部出口经减压阀门V1后连接在低温闪蒸罐（5）的中部入口上；
低温闪蒸罐（5）上开有顶部出口和底部出口，低温闪蒸罐顶部出口经板式换热器（2）流道Ⅱ后连接在闪蒸气储存器上，闪蒸气储存器入口处设置有开关阀门，低温闪蒸器底部出口经减压阀门V4后连接在精馏塔（6）中部入口上，精馏塔（6）上开有顶部出口、上部出口和底部出口，精馏塔顶部出口经板式换热器（2）流道Ⅰ后连接在富氮尾气储存器上，在板式换热器（2）流道Ⅰ和富氮尾气储存器相连的管道上设置有开关阀门，精馏塔底部出口经减压阀门V5后再与板式换热器（2）流道Ⅶ入口相连，板式换热器（2）流道Ⅶ出口连接在CO产品储存器上，精馏塔上部出口连接在塔顶冷凝器（7）上；
塔顶冷凝器（7）包括入口E、入口F、出口G和出口H，精馏塔上部出口连接在冷凝器（7）入口F上，冷凝器（7）的出口G连接在精馏塔（6）上部的入口上；
还包括液氮储存器，液氮储存器经减压阀门V7后连接在冷凝器（7）入口E上，冷凝器（7）出口H经板式换热器（2）流道Ⅷ后连接在循环压缩机单元（10）入口上，循环压缩机单元（10）的出口与板式换热器（2）的流道Ⅸ入口相连，板式换热器（2）流道Ⅸ出口通过管道连接在减压阀门V6和冷凝器（7）入口E相连的管道上；
在净化气低温分离器（3）的顶部出口和板式换热器（2）流道Ⅳ相连的管道上开有分支管，该分支管经减压阀门V2后连接在板式换热器（2）流道Ⅴ的入口上，板式换热器（2）流道Ⅴ出口连接在PSA制氢单元（8）的入口上，PSA制氢单元（8）上开有出口C和出口D，PSA制氢单元（8）出口C连接在氢气产品储存器上，PSA制氢单元（8）出口D经解析气压缩机单元（9）后连接在板式换热器（2）流道Ⅵ进口上，板式换热器（2）流道Ⅵ出口连接在解析气低温分离器（4）中部入口上，解析气低温分离器（4）开有顶部出口和底部出口，解析气低温分离器（4）顶部出口通过管道连接在减压阀门V2和板式蒸发器（2）流道Ⅴ入口相连的管道上，解析气低温分离器（4）底部出口经减压阀门V3后连接在减压阀门V1和低温闪蒸器（5）中部入口相连的管道上。
2.根据权利要求1所述的一种低功耗CO深冷分离系统，其特征在于：所述的低温闪蒸罐（5）为一次分离型或蒸发汽提型。
3.根据权利要求1所述的一种低功耗CO深冷分离系统，其特征在于：所述的循环压缩机单元（10）为离心式或活塞式压缩机。
4.根据权利要求1所述的一种低功耗CO深冷分离系统，其特征在于：所述的解析气压缩机单元（9）为离心式或螺杆式压缩机。
5.根据权利要求1所述的一种低功耗CO深冷分离系统，其特征在于：所述的解析气压缩机单元（9）和循环压缩机单元（10）为电机驱动或汽轮机“一拖二”驱动。
6.根据权利要求1~5任意一项所述的一种低功耗CO深冷分离系统的分离方法，其特征在于：包括以下步骤：
S1、脱碳气储存器中装有脱碳气，脱碳气中含水、甲醇和CO2杂质，脱碳气进入脱碳气净化单元（1）中被脱除水、甲醇和CO2杂质，变为净化气，净化气进入板式换热器（2）流道III被冷却为气相净化气和液相净化气，气相净化气和液相净化气一起进入净化气低温分离器（3）分离，分离后的液相净化气从净化气低温器（3）的底部出口进入低温闪蒸罐（5）中，分离后的气相净化气分为两股，一股返回至板式换热器（2）流道Ⅳ复热至常温后进入脱碳气净化单元（1）工作后，最终被富氢尾气储存器收集，另一股气相返回至板式换热器（2）流道V复热至常温后进入PSA制氢单元（8）中，作为PSA制氢单元（8）的原料气，在PSA制氢单元（8）作用下，原料气变为氢气产品和解析气，氢气产品经PSA制氢单元（8）出口C流出后被氢气产品储存器收集，解析气经解析气压缩机（9）压缩后再进入板式换热器（2）流道Ⅵ被冷却，冷却后的解析气进入解析气低温分离器（4）进行分离，分离后的气相解析气和净化气低温器（3）顶部出口的部分净化气混合，一起进入板式换热器（2）的流道V复热，分离后的液相解析气从解析气低温分离器（4）的底部出口进入低温闪蒸罐（5）中；
S2、液相净化气进入低温闪蒸罐（5）中后进行第二次分离，分离后变为气相闪蒸气和液相闪蒸气，气相闪蒸气通过板式换热器（2）流道II复热至常温后被闪蒸气储存器收集，液相闪蒸气被经减压阀门V4减压后送至精馏塔（6）中部，经过精馏塔（6）精馏，精馏塔（6）精馏后得到富氮尾气和CO液体，富氮尾气分为两股，一股富氮尾气返回至板式换热器（2）流道I复热至常温后被富氮尾气储存器收集，另一股富氮尾气通过入口F连接在塔顶冷凝器（7）上，在塔顶冷凝器（7）中被冷凝后从出口G引出，回流至精馏塔（6）的上部入口，CO液体经减压阀门V5减压后返回至板式换热器（2）流道VII复热至常温后被CO产品储存器收集；
S3、液氮储存器中的液氮通过减压阀门V7后经过入口E进入塔顶冷凝器（7），液氮在塔顶冷凝器（7）中被部分气化，液氮中的冷量用于冷却通过入口F进入塔顶冷冷器（7）中的富氮尾气，气化后的氮气经板式换热器（2）流道VIII复热至常温后，再进入循环压缩机单元（10）压缩变成中压氮气，该中压氮气经板式换热器（2）流道Ⅸ、减压阀门V6后与液氮储存器流出的液氮相混合，混合后再一起进入塔顶冷凝器（7）中实现循环。
7.根据权利要求6所述的一种低功耗CO深冷分离系统的分离方法，其特征在于：所述的解析气压缩机单元（9）的排气压力在2.5~4.0MPa.G之间。
8.根据权利要求6所述的一种低功耗CO深冷分离系统的分离方法，其特征在于：所述的解析气压缩机（9）和解析气低温分离器（4）之间设置有板式换热器（2）的流道VI，该流道VI为单独的解析气换热流道。
9.根据权利要求6所述的一种低功耗CO深冷分离系统的分离方法，其特征在于：所述的循环压缩机单元（10）的压缩介质为氮气，进口压力在0.05~0.5MPa.G之间，排气压力在0.6~3.5MPa.G之间。
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