CN106679332A - 一种提高甲烷深冷分离lng收率的系统 - Google Patents
一种提高甲烷深冷分离lng收率的系统 Download PDFInfo
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Abstract
本发明提出一种提高甲烷深冷分离LNG收率的系统，该系统主要是利用冷冻水管网5‑10℃的冷水，给甲烷深冷分离的原料气压缩系统和混合冷剂循环系统输入冷量，通过降低甲烷原料气和混合冷剂的温度，达到优化甲烷精馏塔操作条件和提高分离效率的目的，从而减少塔顶气体中甲醛的含量，提高LNG收率；具体在原料气入分子筛前增加一台冷冻水换热器，在冷剂压缩机出口分离罐气相与液相管线入冷箱前各增加一台冷冻水换热器。该系统不仅提高了甲烷深冷分离LNG的收率，有效地增加LNG的产量，给企业带来可观的经济效益，而且工艺流程简单，操作方便，日常维护费用低。
Description
技术领域
本发明涉及甲烷深冷分离装置，具体属于一种提高甲烷深冷分离LNG收率的系统。
背景技术
甲烷深冷分离主要是利用原料气中各组分的沸点不同，通过物理降温的方法，达到分离甲烷的目的。该装置首先将原料气压缩后进入分子筛脱除其中的微量甲醇和水，再进入冷箱经过板翅式换热器冷却至-157℃，此时大量的甲烷被冷凝下来，气体经精馏塔蒸发、冷凝后，将原料气中的甲烷分离出来，从精馏塔底部出来的液态甲烷产品被送入LNG储罐，精馏塔顶出来的氢气、一氧化碳进入合成工序。
甲烷深冷分离装置能将煤气化和焦化过程所产生的甲烷有效分离，生产出作为清洁能源的LNG产品，同时使进入合成气的惰性气体得到深度净化和精制，提高合成反应率，降低合成压缩机的能耗，减少了废气排放量，具有显著的经济效益和节能环保效益，因此在大型化工项目中应用前景广阔。
如图1为现有原料气压缩系统的示意图，甲烷原料气经压缩机出口冷却器冷却降温至40℃后，进入分子筛过滤器，使后期进入冷箱的温度为38℃左右。
如图2为现有混合冷剂循环系统的示意图，从冷剂压缩机出口冷却器出来的混合冷剂温度为35℃，进入混合冷剂分离罐分离出来的气相直接进入冷箱，液相经第一液相冷剂泵加压后再进入冷箱。
上述流程存在的不足之处：
随着甲烷深冷分离装置负荷的提升和夏季气温升高的影响，实际生产过程中甲烷原料气和混合冷剂进入冷箱的温度降不下来，系统制冷效果差，冷量不足，使精馏塔顶出来的气体甲烷含量偏高，达不到设计要求，造成LNG收率降低，LNG的产量下降。同时进入合成工序的惰性气体含量偏高，合成压缩机的功率变大，驰放气的排放量增加，反应效率下降，不仅污染环境，而且也影响甲醇产量。
发明内容
本发明的目的就在于克服实际运行过程中的缺陷，利用冷冻水管网5-10℃的冷水给原料气压缩系统和混合冷剂循环系统输入冷量，也就是在原料气入分子筛前增加一台冷冻水换热器，在冷剂压缩机出口分离器气相与液相管线入冷箱前各增加一台冷冻水换热器，分别降低甲烷原料气和混合冷剂的温度，实现优化甲烷精馏塔操作条件和减少塔顶气体中甲醛含量的目标，增加LNG的产量。
本发明所采用的技术方案是：一种提高甲烷深冷分离LNG收率的系统，包括原料气压缩系统和混合冷剂循环系统，所述的原料气压缩系统通过管道与压缩机出口冷却器入口相连，压缩机出口冷却器的出口与原料气入口冷冻水换热器相连，原料气入口冷冻水换热器的出口与分子筛入口过滤器入口相连，出口进入分子筛干燥器。
所述的混合冷剂循环系统通过管道与混合冷剂分离罐入口相连，混合冷剂分离罐底部液相通过第一液相冷剂泵与液相冷剂冷冻水换热器入口相连，出口与冷箱入口相连，混合冷剂分离罐顶部气相与冷箱入口相连，在混合冷剂分离罐顶部气相与冷箱入口相连管线上设置切断阀，将混合冷剂分离罐顶部出口与气相冷剂冷冻水换热器入口相连，气相冷剂冷冻水换热器出口与气相冷剂分离罐进口相连，气相冷剂分离罐顶部气相与冷箱入口相连，气相冷剂分离罐底部液相通过第二液相冷剂泵加压进入混合冷剂分离罐。
所述的冷冻水管网的上回水分别与原料气入口冷冻水换热器、气相冷剂冷冻水换热器和液相冷剂冷冻水换热器入出口相连。
在本发明的一个较佳实施例中，冷冻水管网的上水温度为5-10℃。
在本发明的一个较佳实施例中，为了降低原料气进入甲烷主换热器的温度，将压缩机出口冷却器出口与原料气入口冷冻水换热器相连。
在本发明的一个较佳实施例中，混合冷剂分离罐底部液相通过第一液相冷剂泵与液相冷剂冷冻水换热器入口相连，出口与冷箱入口相连。
在本发明的一个较佳实施例中，混合冷剂分离罐顶部气相与冷剂冷冻水换热器相连，冷剂冷冻水换热器出口与气相冷剂分离罐进口相连，气相冷剂分离罐顶部气相与冷箱相连。
在本发明的一个较佳实施例中，为了保证气相冷剂分离罐液位的稳定，在气相冷剂分离罐底部设置第二液相冷剂泵，通过管道与混合冷剂分离罐底部相连。
与现在技术相比，本发明所具有的优点：
1. 工艺流程简单，操作方便，日常维护费用低。
2.优化甲烷精馏塔的操作条件，减少塔顶气体中甲醛的含量，提高了LNG的收率，增加了产量。
3.增加合成气的有效气体成分，提高合成反应率，降低合成压缩机的能耗，减少废气排放。
4.若膨胀机故障需要检修时，通过冷冻水输入的冷量可以减少经济损失。
附图说明
图1为现有原料气压缩系统的示意图
图2为现有混合冷剂循环系统的示意图
图3为本发明的结构示意图
图中： 1为压缩机出口冷却器、2为原料气入口冷冻水换热器、3为分子筛入口过滤器、4为混合冷剂分离罐、5为气相冷剂冷冻水换热器、6为气相冷剂分离罐、7为第二液相冷剂泵、8为第一液相冷剂泵、9为液相冷剂冷冻水换热器、10为冷箱。
具体实施方式
以下所述的实施例详细说明了本发明，但本发明不仅限于以下实施例。下面结合附图对本发明的较佳实施例进行详细阐述，以使本发明的优点和特征能更易于被本领域技术人员理解，从而对本发明的保护范围做出更为清楚明确的界定。
如图3所示一种提高甲烷深冷分离LNG收率的系统，包括原料气压缩系统和混合冷剂循环系统，所述的原料气压缩系统通过管道与压缩机出口冷却器1入口相连，压缩机出口冷却器1的出口与原料气入口冷冻水换热器2相连，原料气入口冷冻水换热器2的出口与分子筛入口过滤器3入口相连，出口进入分子筛干燥器。
所述的混合冷剂循环系统通过管道与混合冷剂分离罐4入口相连，混合冷剂分离罐4底部液相通过第一液相冷剂泵8与液相冷剂冷冻水换热器9入口相连，出口与冷箱10入口相连，混合冷剂分离罐4顶部气相与冷箱10入口相连，在混合冷剂分离罐4顶部气相与冷箱10入口相连管线上设置切断阀，将混合冷剂分离罐4顶部出口与气相冷剂冷冻水换热器5入口相连，气相冷剂冷冻水换热器5出口与气相冷剂分离罐6进口相连，气相冷剂分离罐6顶部气相与冷箱10入口相连，气相冷剂分离罐6底部液相通过第二液相冷剂泵7加压进入混合冷剂分离罐4。
所述冷冻水管网的上水管线分别与原料气入口冷冻水换热器2、气相冷剂冷冻水换热器5和液相冷剂冷冻水换热器9入口相连，出口管线与冷冻水回水管网相连。
本发明的具体实施例：在原料气压缩系统中，从压缩机出口冷却器出来的原料气温度：40℃，压力：4.85Mpa，流量：240000Nm³/h，进入原料气入口冷冻水换热器降温至15℃后，再送入分子筛入口过滤器。
在混合冷剂循环系统中，从冷剂压缩机出口冷却器出来的混合冷剂温度：35℃，压力：3.40Mpa， 流量：280000Kg/h，进入混合冷剂分离罐，分离出来的气相冷剂通过关闭切断阀不直接进入冷箱，先进入气相冷剂冷冻水换热器将温度降至15℃后，依靠自身压力送入气相冷剂分离罐进一步分离，分离的气相再进入冷箱，分离的液相通过第二液相冷剂泵加压进入混合冷剂分离罐；混合冷剂分离罐分离的液相，通过第一液相冷剂泵送入液相冷剂冷冻水换热器降温至12℃，再进入冷箱。
若进入甲烷的原料气压力：2.5MPa，温度：30℃，流量：220000Nm3/h，甲烷含量：20%。通过增加三台冷冻水换热器，可以降低甲烷原料气和混合冷剂的温度，使甲烷精馏塔的操作条件得到优化，出塔顶去合成工序的气体压力：2.0MPa，温度：20℃，流量：150000Nm3/h，甲烷含量由原来的1.8%降至0.5%，可以使甲烷深冷分离装置LNG的收率提高4-5%。
需要强调的是：以上所述仅为本发明的实施例，并非因此限制本发明的专利范围，凡是利用本发明说明书及附图内容所作的等效结构或等效流程变换，或直接或间接运用在其他相关的技术领域，均同理包括在本发明的专利保护范围内。
Claims (7)
1.一种提高甲烷深冷分离LNG收率的系统，其特征在于，该系统包括原料气压缩系统和混合冷剂循环系统；所述原料气压缩系统中通过管道依次连接压缩机出口冷却器（1）、原料气入口冷冻水换热器（2）、分子筛入口过滤器（3）；所述混合冷剂循环系统中通过管道依次连接混合冷剂分离罐（4）、气相冷剂冷冻水换热器（5）、气相冷剂分离罐（6）、第二液相冷剂泵（7）、第一液相冷剂泵（8）、液相冷剂冷冻水换热器（9）、冷箱（10）；其中，冷冻水管网的上回水分别与原料气入口冷冻水换热器（2）、气相冷剂冷冻水换热器（5）和液相冷剂冷冻水换热器（9）入出口相连。
2.根据权利要求1所述的一种提高甲烷深冷分离LNG收率的系统，其特征在于：所述的原料气压缩系统通过管道与压缩机出口冷却器（1）入口相连，压缩机出口冷却器（1）的出口与原料气入口冷冻水换热器（2）相连，原料气入口冷冻水换热器（2）的出口与分子筛入口过滤器（3）入口相连，出口进入分子筛干燥器。
3.根据权利要求1所述的一种提高甲烷深冷分离LNG收率的系统，其特征在于：所述的混合冷剂循环系统通过管道与混合冷剂分离罐（4）入口相连，混合冷剂分离罐（4）顶部气相与冷箱(10)入口相连，混合冷剂分离罐（4）底部液相通过第一液相冷剂泵（8）与液相冷剂冷冻水换热器（9）入口相连，出口与冷箱(10)入口相连。
4.根据权利要求1所述的一种提高甲烷深冷分离LNG收率的系统，其特征在于：所述的原料气压缩系统和混合冷剂循环系统中共设置三台冷冻水换热器，通过冷冻水管网的上水管线分别与原料气入口冷冻水换热器（2）、气相冷剂冷冻水换热器（5）和液相冷剂冷冻水换热器（9）入口相连，出口管线与冷冻水回水管网相连。
5.根据权利要求3所述的一种提高甲烷深冷分离LNG收率的系统，其特征在于：所述的混合冷剂分离罐（4）顶部气相与冷箱(10)入口相连管线上设置切断阀，将混合冷剂分离罐（4）顶部出口与气相冷剂冷冻水换热器（5）入口相连，气相冷剂冷冻水换热器（5）出口与气相冷剂分离罐（6）进口相连，气相冷剂分离罐（6）顶部气相与冷箱入口相连，气相冷剂分离罐（6）底部液相通过第二液相冷剂泵（7）加压进入混合冷剂分离罐（4）。
6.根据权利要求1所述的一种提高甲烷深冷分离LNG收率的系统，其特征在于：所述冷冻水管网的上水温度为5-10℃。
7.根据权利要求5所述的一种提高甲烷深冷分离LNG收率的系统，其特征在于：所述的气相冷剂分离罐（6）底部设置第二液相冷剂泵（7），通过管道与混合冷剂分离罐（4）底部相连。
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