CN106766674B - 一种异丁烷脱氢制异丁烯项目的冷箱深冷分离方法 - Google Patents

一种异丁烷脱氢制异丁烯项目的冷箱深冷分离方法 Download PDF

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CN106766674B
CN106766674B CN201611130339.9A CN201611130339A CN106766674B CN 106766674 B CN106766674 B CN 106766674B CN 201611130339 A CN201611130339 A CN 201611130339A CN 106766674 B CN106766674 B CN 106766674B
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韦小雄
余景羽
胡明辉
秦燕
张淑文
张宽
吴嘉
单悌禄
吴杰
许路军
周寒秋
林彬彬
孙志广
李宽彪
郑蕴涵
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Hang Yang Group Co ltd
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Abstract

一种异丁烷脱氢制异丁烯项目的冷箱深冷分离方法，所述方法是通过由四台板翅式换热器、六台气液分离器、一台闪蒸罐、一台膨胀机组、一台压缩机组和一台低温泵组成的冷箱深冷分离系统来实现，第一板翅式换热器设有一个热流通道和两个冷流通道，第一进料经过第一板翅式换热器热流通道被冷却后进入第二板翅式换热器的热流通道；第一进料出第二板翅式换热器的热流通道后进入第一气液分离器，第一气液分离器分离出来的气体物流进入第三板翅式换热器被冷却再与第二气液分离器相连；第二气液分离器分离出的气体分成两股物流，其中循环气进入膨胀机组膨胀端，经膨胀后进入第三气液分离器；第三气液分离器分离出的气体也分成两股物流，其中一股闪蒸气产品和第二气液分离器分离出来的液体一同进入第四气液分离器，然后再进第三板翅式换热器的流量通道。

Description

一种异丁烷脱氢制异丁烯项目的冷箱深冷分离方法
技术领域
本发明涉及的是异丁烷脱氢制异丁烯项目的冷箱深冷分离方法，主要适用于催化工艺的异丁烷脱氢制异丁烯项目中对进料在细分的低温区域进行有效分离以及能量回收的深冷分离技术领域。
背景技术：
异丁烯是用于合成聚异丁烯橡胶、丁基橡胶、异戊二烯的主要单体，也广泛用作医药、农药、抗氧剂、合成高级润滑油、汽油添加剂等和其他精细化工产品的主要原料，是一种重要的石油化工原料。通常异丁烯是由炼厂气和裂解C4馏分中获得，异丁烷脱氢制异丁烯是异丁烷在催化剂的作用下脱氢生成异丁烯的工艺。因此该工艺提供了一种新的技术路径，即以异丁烷替代各种馏分油为原料来集中生产异丁烯。异丁烯制备包括C4馏分分离法、离子交换法、甲基叔丁基醚法、工业异丁烯提纯法和异丁烷脱氢等工艺。相比较而言，异丁烷脱氢具有操作成本低、产品质量好、收率高、转化率高、副产物少等优点，越来越成为市场追逐的生产工艺。异丁烷脱氢工艺包括多种，应用最广的为UOP的Oleflex工艺和Lummus的Catofin工艺，前者对异丁烷纯度要求更高，投资少，操作容易，而后者对异丁烷纯度要求低，转化率高，但投资大，催化剂寿命短。目前，Oleflex工艺在全球异丁烷脱氢生产装置中占据优势，这种工艺技术中一个重要的组成部分是物料的深冷分离过程，冷箱作为物料深冷分离的重要设备在分离过程中起到了关键作用。
发明内容
本发明的目的在于解决现有技术存在的不足，提供了一种能耗低、效率高、操作方便、投资少的催化工艺异丁烷脱氢制异丁烯项目的冷箱深冷分离方法，这种方法充分利用了冷量的合理分配，实现了各个板翅式换热器优异的换热性能，节省了能耗。
本发明的目的是通过如下深冷分离技术方法完成的，本发明所述的异丁烷脱氢制异丁烯项目的冷箱深冷分离方法，该方法是由四台板翅式换热器、六台气液分离器、一台闪蒸罐、一台膨胀增压机组、一台压缩机组和一台低温泵组成的深冷分离系统来实现的，所述的第一板翅式换热器设有一个热流通道和两个冷流通道，其中温度为35~50℃的第一进料经过第一板翅式换热器的热流通道被冷却至-10~-20℃后，进入第二板翅式换热器热流通道；
所述第一进料出第二板翅式换热器的热流通道后进入第一气液分离器，第一分离器分离出来的气体物流进入第三板翅式换热器被冷却到-80~-95℃后，再与第二气液分离器相连；
所述第二气液分离器分离出的气体分成两股物流：一股干气产品，一股循环气；循环气进入膨胀机组膨胀端，压力由0.45~0.6MPaG膨胀到0.2~0.35MPaG、温度在-80~-95℃后进入第三气液分离器；
所述第三气液分离器分离出的气体也分成两股物流：一股闪蒸气产品，一股循环氢气；闪蒸气产品和第二气液分离器分离出来的液体一同进入第四气液分离器，然后再进第三板翅式换热器的流量通道；
所述第三板翅式换热器设置有两个热流通道和三个冷流通道，第四板翅式换热器设置有一个热流通道和三个冷流通道；第二进料经过第四板翅式换热器的热流通道被冷却到-10~-25℃后分成两股，一股占总流量5%~20%比例的物流进第三板翅式换热器的热流通道，被冷却到-80~-95℃后节流降压与所述的循环氢气混合，再进入第三板翅式换热器的冷流通道复温后连接第五气液分离器；另一股占80%~95%比例的物流经过节流降压后也进入第五气液分离器；
所述第五气液分离器分离出的气体和液体同时进入第一板翅式换热器的冷流通道复温后，作为冷箱深冷分离出的第一产物输送到下游工艺中。
作为优选，所述的干气产品经过第三板翅式换热器复温后分成两股：一股进入第一板翅式换热器的冷流通道，另一股进入第四板翅式换热器的冷流通道，该两股流分别复温到30~45℃后再混合成一股物流，并经过膨胀机组的增压端加压降温后作为冷箱深冷分离出的第二产物输送到下游工艺中。
作为优选，所述的第一气液分离器和第三气液分离器分离出的液体通过阀门节流后进入闪蒸罐，经过第四气液分离器的物流最终也进入到闪蒸罐中，闪蒸罐在-15~-30℃下分离出的液体进低温泵，经加压后连接第四板翅式换热器的冷流通道，复温到25~40℃后作为冷箱深冷分离出的第四产物；闪蒸罐分离出来的气体进第四板翅式换热器的冷流通道也复温到25~40℃后作为冷箱深冷分离出的第三产物。
作为优选，所述的第二板翅式换热器的冷源是由丙烯冷剂提供，压力为1.5~2.5MPaG、温度为25~40℃的丙烯液体经过阀门节流后进入第六气液分离器，分离出的低温丙烯液体进入第二板翅式换热器的冷流通道形成热虹吸现象提供冷量，第六气液分离器分离出的气体返回压缩机组入口，丙烯气体通过压缩降温后形成所述压力和温度的丙烯液体，实现丙烯冷剂的循环使用。
本发明所述的冷箱深冷分离技术方法在进料为两股的前提下分离出四股产物，这四股产物都能满足催化工艺的异丁烷脱氢制异丁烯项目下游工艺的要求，并且C4产品的回收率能达到99.9%。
本发明具有工艺流程简单易懂、设备数量少、操作方便、C4产品的收率高、能耗低、经济性优良等特点。
附图说明：
图1是本发明的流程示意简图。
具体实施方式
下面将结合附图对本发明作详细的介绍：图1所示，本发明异丁烷脱氢制异丁烯项目的冷箱深冷分离方法，所述的方法是通过由四台板翅式换热器、六台气液分离器、一台闪蒸罐、一台膨胀增压机组、一台压缩机组和一台低温泵组成的深冷分离系统来实现的。
第一板翅式换热器E1设有一个热流通道和两个冷流通道，其中温度为35~50℃的第一进料经过第一板翅式换热器E1的热流通道被冷却至-10~-20℃后进入第二板翅式换热器E2热流通道；
所述第一进料出第二板翅式换热器E2的热流通道后进入第一气液分离器V1，第一气液分离器V1分离出来的气体物流进入第三板翅式换热器E3的热流通道，被冷却到-80~-95℃后再与第二气液分离器V2相连；
所述第二气液分离器V2分离出的气体分成两股物流：一股干气产品，一股循环气；循环气进入膨胀机组膨胀端T1，压力由0.45~0.6MPaG膨胀到0.2~0.35MPaG、温度为-80~-95℃后进入第三气液分离器V3；
所述第三气液分离器V3分离出的气体也分成两股物流：一股闪蒸气产品，一股循环氢气；闪蒸气产品和第二气液分离器V2分离出来的液体一同进入第四气液分离器V4，然后再进第三板翅式换热器E3的流量通道；
所述第三板翅式换热器E3设置有两个热流通道和三个冷流通道，第四板翅式换热器E4设置有一个热流通道和三个冷流通道；第二进料经过第四板翅式换热器E4的热流通道被冷却到-10~-25℃后分成两股，一股占总流量的5%~20%比例的物流进第三板翅式换热器E3的热流通道被冷却到-80~-95℃后节流降压与所述的循环氢气混合，再进入第三板翅式换热器E3的冷流通道复温后连接第五气液分离器V5；另一股占80%~95%比例的物流经过节流降压后也进入第五气液分离器V5；
所述第五气液分离器V5分离出的气体和液体同时进入第一板翅式换热器E1的冷流通道复温后作为冷箱深冷分离出的第一产物输送到下游工艺中。
图中所示，所述的干气产品经过第三板翅式换热器E3复温后分成两股：一股进入第一板翅式换热器E1的冷流通道，另一股进入第四板翅式换热器E4的冷流通道，该两股流分别复温到30~45℃后再混合成一股物流，并经过膨胀机组的增压端C1加压降温后作为冷箱深冷分离出的第二产物输送到下游工艺中。
本发明所述的第一气液分离器V1和第三气液分离器V3分离出的液体通过阀门节流后进入闪蒸罐V7，经过第四气液分离器V4的物流最终也进入到闪蒸罐V7中，闪蒸罐V7在-15~-30℃下分离出的液体进低温泵P1，经加压后连接第四板翅式换热器E4的冷流通道，复温到25~40℃后作为冷箱深冷分离出的第四产物；闪蒸罐V7分离出来的气体进第四板翅式换热器E4的冷流通道也复温到25~40℃后作为冷箱深冷分离出的第三产物。
本发明所述的第二板翅式换热器E2的冷源是由丙烯冷剂提供，压力为1.5~2.5MPaG、温度为25~40℃的丙烯液体经过阀门节流后进入第六气液分离器V6，分离出的低温丙烯液体进入第二板翅式换热器E2的冷流通道形成热虹吸现象提供冷量，第六气液分离器V6分离出的气体返回压缩机组C2入口，丙烯气体通过压缩降温后形成所述压力和温度的丙烯液体，实现丙烯冷剂的循环使用。

Claims (4)

1.一种异丁烷脱氢制异丁烯项目的冷箱深冷分离方法，所述的方法是通过由四台板翅式换热器、六台气液分离器、一台闪蒸罐、一台膨胀机组、一台压缩机组和一台低温泵组成的冷箱深冷分离系统来实现，其特征在于：第一板翅式换热器设有一个热流通道和两个冷流通道，其中温度为35~50℃的第一进料经过第一板翅式换热器热流通道被冷却至-10~-20℃后进入第二板翅式换热器的热流通道；
所述第一进料出第二板翅式换热器的热流通道后进入第一气液分离器，第一气液分离器分离出来的气体物流进入第三板翅式换热器被冷却到-80~-95℃后、再与第二气液分离器相连；
所述第二气液分离器分离出的气体分成两股物流：一股干气产品，一股循环气；循环气进入膨胀机组膨胀端，压力由0.45~0.6MPaG膨胀到0.2~0.35MPaG、温度-80~-95℃后进入第三气液分离器；
所述第三气液分离器分离出的气体也分成两股物流：一股闪蒸气产品，一股循环氢气；闪蒸气产品和第二气液分离器分离出来的液体一同进入第四气液分离器，然后再进第三板翅式换热器的流量通道；
所述第三板翅式换热器设置有两个热流通道和三个冷流通道，第四板翅式换热器设置有一个热流通道和三个冷流通道；第二进料经过第四板翅式换热器的热流通道被冷却到-10~-25℃后分成两股，一股占总流量5%~20%比例的物流进第三板翅式换热器的热流通道，被冷却到-80~-95℃后节流降压与上述的循环氢气混合，再进入第三板翅式换热器的冷流通道，复温后连接第五气液分离器；另一股占80%~95%比例的物流经过节流降压后也进入第五气液分离器；
所述第五气液分离器分离出的气体和液体同时进入第一板翅式换热器的冷流通道，复温后作为冷箱深冷分离出的第一产物输送到下游工艺中。
2.根据权利要求1所述的异丁烷脱氢制异丁烯项目的冷箱深冷分离方法，其特征在于：所述的干气产品经过第三板翅式换热器复温后分成两股：一股进入第一板翅式换热器的冷流通道，另一股进入第四板翅式换热器的冷流通道，该两股流分别复温到30~45℃后再混合成一股物流，并经过膨胀机组的增压端加压降温后作为冷箱深冷分离出的第二产物输送到下游工艺中。
3.根据权利要求1所述的异丁烷脱氢制异丁烯项目的冷箱深冷分离方法，其特征在于：第一气液分离器和第三气液分离器分离出的液体通过阀门节流后进入闪蒸罐，经过第四气液分离器的物流最终也进入到闪蒸罐中，闪蒸罐在-15~ -30℃下分离出的液体进低温泵，经加压后连接第四板翅式换热器的冷流通道，复温到25~40℃后作为冷箱深冷分离出的第四产物；闪蒸罐分离出来的气体进第四板翅式换热器的冷流通道也复温到25~40℃后作为冷箱深冷分离出的第三产物。
4.根据权利要求1所述的异丁烷脱氢制异丁烯项目的冷箱深冷分离方法，其特征在于：第二板翅式换热器的冷源是由丙烯冷剂提供，压力为1.5~2.5MPaG、温度为25~40℃的丙烯液体经过阀门节流后进入第六气液分离器，分离出的低温丙烯液体进入第二板翅式换热器的冷流通道形成热虹吸现象提供冷量，第六气液分离器分离出的气体返回压缩机组入口，丙烯气体通过压缩降温后形成上述压力温度的丙烯液体，实现丙烯冷剂的循环使用。
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