CN105695015B - 一种新型天然气脱重烃装置及方法 - Google Patents

一种新型天然气脱重烃装置及方法 Download PDF

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CN105695015B
CN105695015B CN201610193934.0A CN201610193934A CN105695015B CN 105695015 B CN105695015 B CN 105695015B CN 201610193934 A CN201610193934 A CN 201610193934A CN 105695015 B CN105695015 B CN 105695015B
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heavy hydrocarbon
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马忠
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Sichuan Shudao Equipment Technology Co.,Ltd.
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成都深冷液化设备股份有限公司
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Abstract

本发明涉及一种新型天然气脱重烃装置及方法，该装置包括换热器（1）、LNG闪蒸罐（2）、脱重烃洗涤塔（3）、重烃稳定塔（4）、LNG循环泵（5）和MR分离器（6），所述的脱重烃洗涤塔（3）的出口与LNG闪蒸罐（2）的入口连接，所述的LNG闪蒸罐（2）的出口通过LNG循环通道（26）依次与LNG循环泵（5）和脱重烃洗涤塔（3）的入口连接，所述的脱重烃洗涤塔（3）的出口还通过重烃循环通道（9）与重烃稳定塔（4）的入口连接，所述的重烃稳定塔（4）的出口通过天然气通道III（17）与LNG闪蒸罐（2）的入口连接。本发明具有操作性强、生产成本低、降低能耗、经济效益好等优点。

Description

一种新型天然气脱重烃装置及方法
技术领域
本发明涉及天然气净化技术领域，特别是一种新型天然气脱重烃装置及方法。
背景技术
目前，用于天然气液化装置的天然气主要有常规天然气（油气藏）和非常规天然气（煤层气、页岩气等）。在天然气液化过程中，由于原料气组分相对复杂，重烃含量变化较大，在低温环境下会造成液化冷箱中重烃含量增多，若不及时对重烃进行脱除处理，就会造成冷箱及管道堵塞与冻结等问题，因此，必须在冷凝液化之前或者在冷凝过程中将其分离脱除。
目前，常用的脱重烃技术主要有: 活性炭吸附法、低温重烃洗涤法等方法。活性炭吸附法是利用活性炭分子吸附选择能力强以及低分压下的高吸附特性对重烃进行的吸附去除。中国专利号：CN201320862991.5公布了一种天然气脱重烃装置，该专利所述的工艺采用活性炭、耐水硅胶混合物层等吸附剂的复合床层脱除原料气中的重烃，且采用三塔等压吸附流程脱重烃塔的再生气来自原料气。但是，该工艺受到固体吸附剂饱和度、吸附容度及再生程度的限制，不适于大处理量以及重烃含量高的装置；此外，该工艺增设了再生气加热器，且该装置的再生气由原料气降压取得，这样造成了整个原料气进冷箱的压力下降，增加了液化过程中的能耗。洗涤法是利用重烃在C2~i-C5具有较高的溶解度，而到达脱除重烃的一种方法。中国专利号：CN1743418A 提出了重烃吸收脱除天然气中重烃的方法，该方法采用原料气自身冷凝出重烃（主要是C2~i-C5）来洗涤原料气中的重烃。但是，由于洗涤法脱除重烃，受原料气组分影响较大，当原料气组分中C2~i-C5较少时，洗涤法效果不理想，并不能彻底脱除重烃。
发明内容
本发明的目的在于克服现有技术的缺点，提供一种新型天然气脱重烃装置及方法，该装置及方法具有较强的操作性、生产成本低；在脱除重烃的同时又将冷量回收，降低能耗；增加重烃稳定塔和尾气再液化，有利于回收溶解在重烃中C1~C4，能获取更大的经济效益。
本发明的目的通过以下技术方案来实现：一种新型天然气脱重烃装置，它包括换热器、LNG闪蒸罐、脱重烃洗涤塔、重烃稳定塔、LNG循环泵和MR分离器，所述的换热器内设置有天然气通道I、天然气通道II、天然气通道III和重烃循环通道，所述的换热器外设置有天然气通道Ⅳ，所述的天然气通道I和天然气通道Ⅳ均与脱重烃洗涤塔的入口连接，所述的脱重烃洗涤塔的出口通过天然气通道II与LNG闪蒸罐的入口连接，所述的LNG闪蒸罐的出口通过LNG循环通道依次与LNG循环泵和脱重烃洗涤塔的入口连接，所述的LNG闪蒸罐的出口处还连接有LNG输出通道和BOG输出通道，所述的脱重烃洗涤塔的出口还通过重烃循环通道与重烃稳定塔的入口连接，所述的重烃稳定塔的出口通过天然气通道III与LNG闪蒸罐的入口连接，所述的重烃稳定塔的出口处还连接有重烃输出通道。
优选地，所述的换热器内还设置有气相冷剂通道、气液混合相冷剂通道和液相冷剂通道，所述的气相冷剂通道与MR分离器的入口连接，MR分离器的出口与气液混合相冷剂通道连接，所述的液相冷剂通道与气液混合相冷剂通道连通。
优选地，所述的重烃稳定塔的顶部设置有冷凝器，所述的重烃稳定塔的底部设置有再沸器。
优选地，所述的天然气通道Ⅳ上设置有调节阀a和温度数字控制器。
优选地，所述的重烃循环通道上设置有调节阀h和液位数字控制器B。
优选地，所述的LNG输出通道上设置有调节阀f和液位数字控制器A。
优选地，所述的LNG循环通道上设置有调节阀g和流量数字控制器。
优选地，所述的LNG闪蒸罐中设置有除沫器。
优选地，所述的脱重烃洗涤塔中设置有除沫器。
优选地，所述的脱重烃洗涤塔为填料塔或板式塔。
优选地，所述的重烃稳定塔为填料塔或板式塔。
优选地，所述的再沸器为内置式再沸器、釜式再沸器或热虹吸式再沸器。
优选地，所述的换热器为板式换热器、绕管式换热器或管壳式换热器。
优选地，所述的天然气通道I、天然气通道II、天然气通道III、重烃循环通道、气相冷剂通道、气液混合相冷剂通道和液相冷剂通道相互平行。
优选地，所述的气相冷剂通道和液相冷剂通道分别为高压气相冷剂通道和高压液相冷剂通道。
一种新型天然气脱重烃的方法，它包括以下步骤：
S1、经脱酸、干燥合格的天然气在A点分成两股，第一股进入换热器内的天然气通道I中进行预冷，第二股经过天然气通道Ⅳ与进入换热器内被预冷的第一股天然气汇合后进入脱重烃洗涤塔内；
S2、天然气从脱重烃洗涤塔顶部输出进入天然气通道II内冷却、冷凝、液化后进入LNG闪蒸罐内；
S3、在 LNG闪蒸罐分离出的BOG经BOG输出通道输出；得到的LNG一部分经LNG输出通道输出，另一部分经LNG循环泵加压送入脱重烃洗涤塔顶部；
S4、被加压送入脱重烃洗涤塔内的LNG经所述的脱重烃洗涤塔处理后得到的重烃进入重烃循环通道进行复热，然后经重烃循环通道输送到重烃稳定塔内；
S5、经重烃稳定塔处理得到的C1~C4经过天然气通道III被冷却、冷凝、液化后与步骤S2中得到的液化天然气一起进入LNG闪蒸罐，经重烃稳定塔处理得到的C5 +经重烃输出通道输出。
优选地，所述的换热器内设置有气相冷剂通道、气液混合相冷剂通道和液相冷剂通道，所述的气相冷剂依次进入气相冷剂通道内冷却、进入MR分离器气液分离后得到的气相和液相被输送到气液混合相冷剂通道内；液相冷剂进入液相冷剂通道内冷却后也进入气液混合相冷剂通道内。
优选地，所述的步骤S5中经重烃稳定塔处理得到的C1~C4进入天然气通道III被冷却、冷凝、液化后也可外输另用。
本发明具有以下优点：
1、有效防止冷箱冻堵：本发明采用产品LNG经加压后打入脱重烃洗涤塔顶部，对进入脱重烃洗涤塔底部的原料气进行洗涤，可有效的将原料气中的重烃进行脱除，防止冷箱冻堵；
2、降低能耗、降低投资成本：本发明中原料气进入脱重烃洗涤塔的温度可通过调节阀a进行调节，替代了常规重烃洗涤法所采用的蒸发器，且脱重烃洗涤塔顶部采用低温的LNG作为洗涤液，替代了常规重烃洗涤法的冷凝器，与常规重烃洗涤法装置相比，液化工厂总能耗降低5%~8%，降低了投资成本；且在脱除重烃的同时又将冷量回收，进一步降低能耗；
3、增获副产品、经济可靠：本发明采用了重烃稳定塔将低温洗涤后的重烃进行分离，有利于回收溶解在重烃中的C1~C4，得到轻油副产品，经济可靠，能获取更大的经济效益；
4、提高天然气液化率：本发明对重烃稳定塔顶部出来的轻组分进行了回收液化，提高了天然气的液化率，能获取更大的经济效益；
5、此外，该装置还具有较强操作性、生产成本低等优点。
附图说明
图1 为本发明具体实施方式中的结构示意图；
图中：1-换热器，2- LNG闪蒸罐，3-脱重烃洗涤塔，4-重烃稳定塔，5- LNG循环泵，6-MR分离器，7-调节阀a，8-天然气通道Ⅳ，9-重烃循环通道，10-天然气通道I，11-气相冷剂通道，12-气液混合相冷剂通道，13-液相冷剂通道，14-调节阀b，15-调节阀c，16-天然气通道II，17-天然气通道III，18-调节阀d，19-调节阀e，20-液位数字控制器A，21-调节阀f，22-LNG输出通道，23-调节阀g，24-流量数字控制器，25-BOG输出通道，26-LNG循环通道，27-调节阀h，28-液位数字控制器B，29-温度数字控制器，30-重烃输出通道，31-调节阀i，32-再沸器，33-冷凝器，34-调节阀j。
具体实施方式
下面结合附图对本发明做进一步的描述，但本发明的保护范围不局限于以下所述。
如图1所示，一种新型天然气脱重烃装置，它包括换热器1、LNG闪蒸罐2、脱重烃洗涤塔3、重烃稳定塔4、LNG循环泵5和MR分离器6。所述的换热器1为板式换热器，所述的脱重烃洗涤塔3为填料塔，所述的重烃稳定塔4为板式塔，所述的LNG闪蒸罐2与脱重烃洗涤塔3中均分别设置有除沫器。
所述的换热器1内设置有平行的天然气通道I10、天然气通道II16、天然气通道III17、重烃循环通道9、气相冷剂通道11、气液混合相冷剂通道12和液相冷剂通道13，所述的换热器1外设置有天然气通道Ⅳ8，所述的气相冷剂通道11和液相冷剂通道13分别为高压气相冷剂通道和高压液相冷剂通道。
所述的LNG闪蒸罐2上设置有LNG入口、BOG气相出口和LNG液相出口B；所述的脱重烃洗涤塔3上设置LNG入口D、天然气入口E、重烃出口G和天然气出口F；所述的重烃稳定塔4上设置有重烃入口H、轻质油出口I和天然气出口J；所述的MR分离器6上设置有冷剂入口K、顶部气相冷剂出口L和底部液相冷剂出口M。
所述的天然气通道I10和天然气通道Ⅳ8均与脱重烃洗涤塔3的天然气入口E连接，天然气通道Ⅳ8上设置有调节阀a7和温度数字控制器29；所述的脱重烃洗涤塔3的顶部天然气出口F通过天然气通道II16与LNG闪蒸罐2的LNG入口连接，天然气通道II16上设置有调节阀d18。所述的LNG闪蒸罐2的LNG液相出口B通过LNG循环通道26依次与LNG循环泵5和脱重烃洗涤塔3的LNG入口D连接，所述的LNG循环通道26上设置有调节阀g23和流量数字控制器24；所述的LNG闪蒸罐2的LNG液相出口B处还连接有LNG输出通道22，LNG输出通道22上设置有调节阀f21和液位数字控制器A20；LNG闪蒸罐2的顶部BOG气相出口连接有BOG输出通道25。
所述的脱重烃洗涤塔3的底部重烃出口G还通过重烃循环通道9与重烃稳定塔4的重烃入口H连接，重烃循环通道9上设置有调节阀h27和液位数字控制器B28。所述的重烃稳定塔4的顶部天然气出口J通过天然气通道III17与LNG闪蒸罐2的LNG入口连接，天然气通道III17上设置有调节阀e19和调节阀j34；所述的重烃稳定塔4的底部轻质油出口I处还连接有重烃输出通道30，重烃输出通道30上设置有调节阀i31；重烃稳定塔4的顶部设置有冷凝器33，重烃稳定塔4的底部设置有再沸器32，再沸器32为内置式再沸器。所述的气相冷剂通道11与MR分离器6的冷剂入口K连接，气相冷剂通道11上设置有调节阀c15，MR分离器6的底部液相冷剂出口M和顶部气相冷剂出口L均与气液混合相冷剂通道12连接，所述的液相冷剂通道13与气液混合相冷剂通道12连通，液相冷剂通道13上设置有调节阀b14。
一种新型天然气脱重烃的方法，它包括以下步骤：
S1、经脱酸、干燥合格的天然气在A点分成两股，第一股进入换热器1内的天然气通道I10中进行预冷至-70~-35℃，第二股经过天然气通道Ⅳ8与进入换热器1内被预冷的第一股天然气汇合后从脱重烃洗涤塔3的天然气入口E进入脱重烃洗涤塔3内，原料气进脱重烃洗涤塔3的温度可通过调节阀a7进行调节，脱重烃洗涤塔3内的温度为-65~0℃，脱重烃洗涤塔3的操作压力1~10 Mpag；所述的换热器1内设置有气相冷剂通道11、气液混合相冷剂通道12和液相冷剂通道13，所述的高压气相冷剂进入气相冷剂通道11内冷却至一定温度，再经过调节阀c15节流后，进入MR分离器6气液分离得到的气相和液相，气相和液相从不同的管口进入到气液混合相冷剂通道12内；高压液相冷剂进入液相冷剂通道13内冷却至一定温度，再经调节阀b14节流后也进入气液混合相冷剂通道13内；
S2、天然气从脱重烃洗涤塔3顶部天然气出口F输出进入天然气通道II16内冷却、冷凝、液化，再经调节阀d18节流后，进入LNG闪蒸罐2内；
S3、在 LNG闪蒸罐2分离出的BOG经BOG输出通道25输出；得到的LNG一部分经LNG输出通道22输出，另一部分经LNG循环泵5加压送入脱重烃洗涤塔3顶部，而进入脱重烃洗涤塔3的量可以通过调节阀g23调节；
S4、被加压送入脱重烃洗涤塔3内的LNG经所述的脱重烃洗涤塔3处理后得到的重烃从底部重烃出口G输出进入重烃循环通道9进行复热，然后经重烃循环通道9输送到重烃稳定塔4的中部；重烃稳定塔4的操作压力0.2Mpag~3.5Mpag，重烃稳定塔4塔顶的操作温度-35~40℃，塔底操作温度45~150℃；
S5、经重烃稳定塔4处理得到的C1~C4经顶部天然气出口J输出进入天然气通道III17内冷却、冷凝、液化，再经调节阀19e节流后，与步骤S2中得到的液化天然气一起进入LNG闪蒸罐2，经重烃稳定塔4处理得到的C5 +经重烃输出通道30输出，这样不仅可以得到副产品轻质油，又提高天然气液化率；此外，经重烃稳定塔4处理得到的C1~C4进入天然气通道III17被冷却、冷凝、液化后也可外输另用。

Claims (10)

1.一种新型天然气脱重烃装置，其特征在于，它包括换热器（1）、LNG闪蒸罐（2）、脱重烃洗涤塔（3）、重烃稳定塔（4）、LNG循环泵（5）和MR分离器（6），所述的换热器（1）内设置有天然气通道I（10）、天然气通道II（16）、天然气通道III（17）和重烃循环通道（9），所述的换热器（1）外设置有天然气通道Ⅳ（8），所述的天然气通道I（10）和天然气通道Ⅳ（8）均与脱重烃洗涤塔（3）的入口连接，所述的脱重烃洗涤塔（3）的出口通过天然气通道II（16）与LNG闪蒸罐（2）的入口连接，所述的LNG闪蒸罐（2）的出口通过LNG循环通道（26）依次与LNG循环泵（5）和脱重烃洗涤塔（3）的入口连接，所述的LNG闪蒸罐（2）的出口处还连接有LNG输出通道（22）和BOG输出通道（25），所述的脱重烃洗涤塔（3）的出口还通过重烃循环通道（9）与重烃稳定塔（4）的入口连接，所述的重烃稳定塔（4）的出口通过天然气通道III（17）与LNG闪蒸罐（2）的入口连接，所述的重烃稳定塔（4）的出口处还连接有重烃输出通道（30）。
2.根据权利要求1所述的一种新型天然气脱重烃装置，其特征在于，所述的换热器（1）内还设置有气相冷剂通道（11）、气液混合相冷剂通道（12）和液相冷剂通道（13），所述的气相冷剂通道（11）与MR分离器（6）的入口连接，MR分离器（6）的出口与气液混合相冷剂通道（12）连接，所述的液相冷剂通道（13）与气液混合相冷剂通道（12）连通。
3.根据权利要求1所述的一种新型天然气脱重烃装置，其特征在于，所述的重烃稳定塔（4）的顶部设置有冷凝器（33），所述的重烃稳定塔（4）的底部设置有再沸器（32）。
4.根据权利要求1所述的一种新型天然气脱重烃装置，其特征在于，所述的天然气通道Ⅳ（8）上设置有调节阀a（7）和温度数字控制器（29）。
5.根据权利要求1所述的一种新型天然气脱重烃装置，其特征在于，所述的重烃循环通道（9）上设置有调节阀h（27）和液位数字控制器B（28）。
6.根据权利要求1所述的一种新型天然气脱重烃装置，其特征在于，所述的LNG输出通道（22）上设置有调节阀f（21）和液位数字控制器A（20）。
7.根据权利要求1所述的一种新型天然气脱重烃装置，其特征在于，所述的LNG循环通道（26）上设置有调节阀g（23）和流量数字控制器（24）。
8.根据权利要求1所述的一种新型天然气脱重烃装置，其特征在于，所述的LNG闪蒸罐（2）中设置有除沫器。
9.一种新型天然气脱重烃的方法，其特征在于，它包括以下步骤：
S1、经脱酸、干燥合格的天然气在A点分成两股，第一股进入换热器（1）内的天然气通道I（10）中进行预冷，第二股经过天然气通道Ⅳ（8）与进入换热器（1）内被预冷的第一股天然气汇合后进入脱重烃洗涤塔（3）内；
S2、天然气从脱重烃洗涤塔（3）顶部输出进入天然气通道II（16）内冷却、冷凝、液化后进入LNG闪蒸罐（2）内；
S3、在 LNG闪蒸罐（2）分离出的BOG经BOG输出通道（25）输出；得到的LNG一部分经LNG输出通道（22）输出，另一部分经LNG循环泵（5）加压送入脱重烃洗涤塔（3）顶部；
S4、被加压送入脱重烃洗涤塔（3）内的LNG经所述的脱重烃洗涤塔（3）处理后得到的重烃进入重烃循环通道（9）进行复热，然后经重烃循环通道（9）输送到重烃稳定塔（4）内；
S5、经重烃稳定塔（4）处理得到的C1~C4经过天然气通道III（17）被冷却、冷凝、液化后与步骤S2中得到的液化天然气一起进入LNG闪蒸罐（2），经重烃稳定塔（4）处理得到的C5 +经重烃输出通道（30）输出。
10.根据权利要求9所述的一种新型天然气脱重烃的方法，其特征在于，所述的换热器（1）内设置有气相冷剂通道（11）、气液混合相冷剂通道（12）和液相冷剂通道（13），所述的气相冷剂依次进入气相冷剂通道（11）内冷却、进入MR分离器（6）气液分离后得到的气相和液相被输送到气液混合相冷剂通道（12）内；液相冷剂进入液相冷剂通道（13）内冷却后也进入气液混合相冷剂通道（13）内。
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