CN107084594B - 一种液co循环制冷合成气制甲醇联产lng装置及其使用方法 - Google Patents

一种液co循环制冷合成气制甲醇联产lng装置及其使用方法 Download PDF

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CN107084594B
CN107084594B CN201710287528.5A CN201710287528A CN107084594B CN 107084594 B CN107084594 B CN 107084594B CN 201710287528 A CN201710287528 A CN 201710287528A CN 107084594 B CN107084594 B CN 107084594B
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CN107084594A (zh
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章有虎
陈环琴
李传明
屠长明
廖江芬
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Hangzhou Zhongtai Cryogenic Technology Corp
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Abstract

本发明公开了一种液CO循环制冷合成气制甲醇联产LNG装置及其使用方法。该装置包括换热器、洗涤塔、甲烷精馏塔、分离器、第一节流阀、第二节流阀、第三节流阀、第四节流阀、压缩机、膨胀机、分子筛吸附器、制甲醇管路、CO循环管路及联产LNG管路，所述的甲烷精馏塔塔底内部设有再沸器。采用本发明脱除上游低温甲醇洗工序的净化气体中的CH4，最终制成高纯度碳氢氧比为1:4:1的合成气，用于合成甲醇生产，同时分离出的富甲烷液体经甲烷精馏塔分离后得到LNG。本发明巧妙结合富CO压缩机制冷循环，减少设备投入，降低制冷循环能耗同时提高了装置的总效率。

Description

一种液CO循环制冷合成气制甲醇联产LNG装置及其使用方法
技术领域
本发明涉及化工深冷净化装置，尤其涉及一种液CO循环制冷合成气制甲醇联产LNG装置及其使用方法。
背景技术
甲醇是一种重要的有机化工原料，应用广泛，可以用来生产有机化工产品，而且还可以加入汽油掺烧或代替汽油作为动力燃料以及用来合成甲醇蛋白。随着石油资源的日益减少和甲醇单位成本的降低，用甲醇作为新的石化原料来源已经成为一种趋势。
传统制甲醇联产LNG装置，通常将原料气先进入高压精馏塔，然后再进入低压精馏塔，得到富H2气、富CO气及LNG。这种方法效率低、能耗高、占地大、合成气中驰放气流量大，增加了下道工序的压缩机能耗，生产成本较高。在制冷循环过程中，采用氮气循环制冷和混合冷剂制冷循环，需要另增设备，增加系统的复杂程度。
发明内容
本发明的目的是克服现有技术的不足，提供一种液CO循环制冷合成气制甲醇联产LNG装置及其使用方法
一种液CO循环制冷合成气制甲醇联产LNG装置，其特征在于包括换热器、洗涤塔、甲烷精馏塔、分离器、第一节流阀、第二节流阀、第三节流阀、第四节流阀、压缩机、膨胀机、分子筛吸附器、制甲醇管路、支流b、支流c、支流g、支流h、支流j、支流k、CO循环管路及联产LNG管路，所述的甲烷精馏塔塔底内部设有再沸器；
制甲醇管路穿过分子筛吸附器和换热器与甲烷精馏塔塔底内部的再沸器连接，再沸器出口通过支流b再次穿过换热器与分离器入口连接；
分离器出口分为上下两路，上路通过支流c经换热器与洗涤塔下部连接；洗涤塔底部通过联产LNG管路经第二节流阀穿过换热器与甲烷精馏塔下部连接；下路通过联产LNG管路经第四节流阀与甲烷精馏塔中部连接；
甲烷精馏塔顶部通过CO循环管路穿过换热器与压缩机入口连接，压缩机出口分为支流j和支流k，支流j经换热器与洗涤塔上部连接；支流k穿过换热器和膨胀机接入压缩机入口形成环路；
所述的洗涤塔顶部通过制甲醇管路穿过换热器与外界甲醇合成装置连接。
所述的甲烷精馏塔底部通过联产LNG管路分为支流g和支流h，支流g依次穿过第三节流阀和换热器与外界富甲烷气压缩机连接；支流h依次穿过换热器和第一节流阀与外界LNG产品储罐连接。
所述的压缩机和膨胀机通过CO循环管路组成制冷循环，制冷循环采用CO作为制冷剂，为换热器提供冷源，同时压缩机压缩产生的液态CO输入洗涤塔中，作为洗涤液。
液CO循环制冷合成气制甲醇联产LNG装置，还包括分子筛再生系统、分子筛管路，所述的分子筛吸附器通过分子筛管路与分子筛再生系统连接。
所述的分子筛吸附器有两或三台，其内装分子筛，两台一起使用，大规模生产时，第三台用于再生循环，三台自动切换。
液CO循环制冷合成气制甲醇联产LNG装置的使用方法，包括以下步骤：
1)原料气Q输入分子筛吸附器脱除易冻成分甲醇和二氧化碳，得到的脱甲醇二氧化碳原料气a在换热器中与富氢合成气d、富一氧化碳气i逆流换热冷却，经再沸器到一定温度后部分冷凝，支流b进入分离器；
2)分离器顶部气体支流c经换热器继续冷却进入洗涤塔下部，在洗涤塔中被支流j流入的液态一氧化碳吸收CH、N，得到富氢合成气d，富氢合成气d，从洗涤塔顶部出来经换热器换热回收冷量后，送往外界甲醇合成装置；
3)分离器底部富甲烷液体f和洗涤塔底釜液e分别经第四节流阀和第二节流阀减压后进入甲烷精馏塔，甲烷精馏塔塔底得到LNG，经联产LNG管路分为支流g经第三节流阀减压和换热器过冷送至外界富甲烷气压缩机压缩后送入LNG产品储罐，另一支流h经换热器过冷和第一节流阀减压送至外界LNG产品储罐；
4)甲烷精馏塔塔顶富一氧化碳气i经换热器换热回收冷量后进入压缩机压缩后分成两支，支流j在换热器内过冷后，通入洗涤塔提供回流液，用于洗涤，另一支流k由换热器降温后经膨胀机膨胀后返回换热器提供冷量，再返回压缩机入口进行闭式循环；
采用本发明，先将原料气部分冷凝后在分离器中分离，气体在洗涤塔中经液态CO洗涤形成富氢合成气，送出装置用于制甲醇，剩余釜液与分离器底部富甲烷液态送至甲烷精馏塔联产LNG，整体能耗降低，合成气中驰放气流量减小，减小了下道工序的压缩机能耗。巧妙地将富CO压缩机和制冷循环结合起来，压缩机即是产品压缩机，又为装置提供了冷量，减少了一台动设备，节约投资，提高了装置的总效率，节约能耗。
附图说明
图1为液CO循环制冷合成气制甲醇联产LNG装置示意图；
图2为液CO循环制冷合成气制甲醇联产LNG装置分子筛吸附器示意图；
图中，换热器1、洗涤塔2、甲烷精馏塔3、分离器4、第一节流阀5、第二节流阀6、第三节流阀7、第四节流阀8、压缩机9、膨胀机10、再沸器11、分子筛吸附器12、分子筛再生系统13。
具体实施方式
如图1所示，液CO循环制冷合成气制甲醇联产LNG装置，包括换热器1、洗涤塔2、甲烷精馏塔3、分离器4、第一节流阀5、第二节流阀6、第三节流阀7、第四节流阀8、压缩机9、膨胀机10、分子筛吸附器12、制甲醇管路、支流b、支流c、支流g、支流h、支流j、支流k、CO循环管路及联产LNG管路，所述的甲烷精馏塔3塔底内部设有再沸器11；
制甲醇管路穿过分子筛吸附器12和换热器1与甲烷精馏塔3塔底内部的再沸器11连接，再沸器11出口通过支流b再次穿过换热器1与分离器4入口连接；
分离器4出口分为上下两路，上路通过支流c经换热器1与洗涤塔2下部连接；洗涤塔2底部通过联产LNG管路经第二节流阀6穿过换热器1与甲烷精馏塔3下部连接；下路通过联产LNG管路经第四节流阀8与甲烷精馏塔3中部连接；
甲烷精馏塔3顶部通过CO循环管路穿过换热器1与压缩机9入口连接，压缩机9出口分为支流j和支流k，支流j经换热器1与洗涤塔2上部连接；支流k穿过换热器1和膨胀机10接入压缩机9入口形成环路；
洗涤塔2顶部通过制甲醇管路穿过换热器1与外界甲醇合成装置连接。
甲烷精馏塔3底部通过联产LNG管路分为支流g和支流h，支流g依次穿过第三节流阀7和换热器1与外界富甲烷气压缩机连接；支流h依次穿过换热器1和第一节流阀5与外界LNG产品储罐连接。
压缩机9和膨胀机10通过CO循环管路组成制冷循环，制冷循环采用CO作为制冷剂，为换热器1提供冷源，同时压缩机9压缩产生的液态CO输入洗涤塔2中，作为洗涤液。
如图2所示，分子筛吸附器12通过分子筛管路与分子筛再生系统13连接；
分子筛吸附器有两或三台，其内装分子筛，两台一起使用，大规模生产时，第三台用于再生循环，三台自动切换。
如图2所示，液CO循环制冷合成气制甲醇联产LNG装置的使用方法，包括以下步骤：
1)原料气Q输入分子筛吸附器12脱除易冻成分甲醇和二氧化碳，得到的脱甲醇二氧化碳原料气a在换热器1中与富氢合成气d、富一氧化碳气i逆流换热冷却，经再沸器11到一定温度后部分冷凝，支流b进入分离器4；
2)分离器4顶部气体支流c经换热器1继续冷却进入洗涤塔2下部，在洗涤塔2中被支流j流入的液态一氧化碳吸收CH4、N2，得到富氢合成气d，富氢合成气d，从洗涤塔顶部出来经换热器1换热回收冷量后，送往外界甲醇合成装置；
3)分离器4底部富甲烷液体f和洗涤塔2底釜液e分别经第四节流阀8和第二节流阀6减压后进入甲烷精馏塔3，甲烷精馏塔3塔底得到LNG，经联产LNG管路分为支流g经第三节流阀7减压和换热器1过冷送至外界富甲烷气压缩机压缩后送入LNG产品储罐，另一支流h经换热器1过冷和第一节流阀5减压送至外界LNG产品储罐；
4)甲烷精馏塔3塔顶富一氧化碳气i经换热器1换热回收冷量后进入压缩机9压缩后分成两支，支流j在换热器1内过冷后，通入洗涤塔2提供回流液，用于洗涤，另一支流k由换热器1降温后经膨胀机10膨胀后返回换热器1提供冷量，再返回压缩机9入口进行闭式循环。

Claims (5)

1.一种液CO循环制冷合成气制甲醇联产LNG装置，其特征在于包括换热器(1)、洗涤塔(2)、甲烷精馏塔(3)、分离器(4)、第一节流阀(5)、第二节流阀(6)、第三节流阀(7)、第四节流阀(8)、压缩机(9)、膨胀机(10)、分子筛吸附器(12)、制甲醇管路、支流b、支流c、支流g、支流h、支流j、支流k、CO循环管路及联产LNG管路，所述的甲烷精馏塔(3)塔底内部设有再沸器(11)；
制甲醇管路穿过分子筛吸附器(12)和换热器(1)与甲烷精馏塔(3)塔底内部的再沸器(11)连接，再沸器(11)出口通过支流b再次穿过换热器(1)与分离器(4)入口连接；
分离器(4)出口分为上下两路，上路通过支流c经换热器(1)与洗涤塔(2)下部连接；洗涤塔(2)底部通过联产LNG管路经第二节流阀(6)穿过换热器(1)与甲烷精馏塔(3)下部连接；下路通过联产LNG管路经第四节流阀(8)与甲烷精馏塔(3)中部连接；
甲烷精馏塔(3)顶部通过CO循环管路穿过换热器(1)与压缩机(9)入口连接，压缩机(9)出口分为支流j和支流k，支流j经换热器(1)与洗涤塔(2)上部连接；支流k穿过换热器(1)和膨胀机(10)接入压缩机(9)入口形成环路；甲烷精馏塔(3)底部通过联产LNG管路分为支流g和支流h，支流g依次穿过第三节流阀(7)和换热器(1)与外界富甲烷气压缩机连接；支流h依次穿过换热器(1)和第一节流阀(5)与外界LNG产品储罐连接；
洗涤塔(2)顶部通过制甲醇管路穿过换热器(1)与外界甲醇合成装置连接。
2.根据权利要求1所述的液CO循环制冷合成气制甲醇联产LNG装置，其特征在于所述的压缩机(9)和膨胀机(10)通过CO循环管路组成制冷循环，制冷循环采用CO作为制冷剂，为换热器(1)提供冷源，同时压缩机(9)压缩产生的液态CO输入洗涤塔(2)中，作为洗涤液。
3.根据权利要求1所述的液CO循环制冷合成气制甲醇联产LNG装置，其特征在于还包括分子筛再生系统(13)、分子筛管路，所述的分子筛吸附器(12)通过分子筛管路与分子筛再生系统(13)连接。
4.根据权利要求1或3所述的液CO循环制冷合成气制甲醇联产LNG装置，其特征在于所述的分子筛吸附器(12)有两或三台，其内装分子筛，两台一起使用，大规模生产时，第三台用于再生循环，三台自动切换。
5.一种如权利要求1所述的液CO循环制冷合成气制甲醇联产LNG装置的使用方法，其特征在于包括以下步骤：
1)原料气Q输入分子筛吸附器(12)脱除易冻成分甲醇和二氧化碳，得到的脱甲醇二氧化碳原料气a在换热器(1)中与富氢合成气d、富一氧化碳气i逆流换热冷却，经再沸器(11)到一定温度后部分冷凝，支流b进入分离器(4)；
2)分离器(4)顶部气体支流c经换热器(1)继续冷却进入洗涤塔(2)下部，在洗涤塔(2)中被支流j流入的液态一氧化碳吸收CH4、N2，得到富氢合成气d，富氢合成气d从洗涤塔顶部出来经换热器(1)换热回收冷量后，送往外界甲醇合成装置；
3)分离器(4)底部富甲烷液体f和洗涤塔(2)底釜液e分别经第四节流阀(8)和第二节流阀(6)减压后进入甲烷精馏塔(3)，甲烷精馏塔(3)塔底得到LNG，经联产LNG管路分为支流g经第三节流阀(7)减压和换热器(1)过冷送至外界富甲烷气压缩机压缩后送入LNG产品储罐，另一支流h经换热器(1)过冷和第一节流阀(5)减压送至外界LNG产品储罐；
4)甲烷精馏塔(3)塔顶富一氧化碳气i经换热器(1)换热回收冷量后进入压缩机(9)压缩后分成两支，支流j在换热器(1)内过冷后，通入洗涤塔(2)提供回流液，用于洗涤，另一支流k由换热器(1)降温后经膨胀机(10)膨胀后返回换热器(1)提供冷量，再返回压缩机(9)入口进行闭式循环。
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