CN201662301U - 煤气化装置来原料气甲烷深冷分离装置的换热系统 - Google Patents

煤气化装置来原料气甲烷深冷分离装置的换热系统 Download PDF

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CN201662301U
CN201662301U CN2009203088343U CN200920308834U CN201662301U CN 201662301 U CN201662301 U CN 201662301U CN 2009203088343 U CN2009203088343 U CN 2009203088343U CN 200920308834 U CN200920308834 U CN 200920308834U CN 201662301 U CN201662301 U CN 201662301U
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heat exchanger
nitrogen
main heat
azeotrope
compressor
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周勇
阴红兵
王磊
黄顺泰
彭正春
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Chengdu Shuyuan Coal & Basic Energy Technology Co Ltd
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Abstract

本实用新型公开的煤气化装置来原料气CH4深冷分离装置的换热系统，包括有板翅式主换热器、混合冷剂循环压缩机及氮气循环压缩机，主换热器中布置有原料气通道、混合冷剂通道和氮气通道，其中，从上游煤气化装置来原料气首先在主换热器中换热，然后经过再沸器冷却后再进入主换热器进一步冷却并部分冷凝后到洗涤塔；主换热器中混合冷剂换热通道的进出口分别连至闭式混合冷剂循环的进出口；主换热器中的氮换热通道的进/出口分别连至氮循环压缩机的出/进口。本实用新型由于采用闭式混合冷剂制冷循环和氮气制冷循环组合的方式，同时利用空分补充液氮的方法。这样改善主换热器的传热温差，减少主换热器的不可逆损耗，降低整套深冷分离装置的能耗。

Description

煤气化装置来原料气甲烷深冷分离装置的换热系统 
技术领域
本实用新型涉及一种煤气化装置来原料气的CH4深冷分离装置的换热系统，属于低温气体分离技术领域。 
背景技术
目前化工厂的煤气化装置来的原料气，基本组分为CO、CH4、H2，由于其中甲烷气的存在，对利用原料气合成氨或合成甲醇非常不利，影响产品的合成率并增加能耗。所以要求将CH4和CO，H2分离，这样就要将原料气在换热器内冷却到-165℃～-160℃。以前技术多采用单一的闭式混合冷剂制冷循环或氮气膨胀制冷循环。 
实用新型内容
本实用新型的目的在于：提供一种可有效分离基本组分为一氧化碳，氢气和甲烷的原料气、分离液化甲烷（LNG）作为清洁能源，具有环保、节能、成本低等特点的煤气化装置来原料气的CH4深冷分离装置的换热系统。 
本实用新型的技术方案是： 
一种煤气化装置来原料气甲烷深冷分离装置的换热系统，包括有板翅式主换热器、闭式混合冷剂循环压缩机及氮气循环压缩机，主换热器中布置有原料气通道、混合冷剂通道和氮气通道，其中，主换热器中的原料气通道包括原料气进口通道、原料气换热通道和返流的合成气通道，氮气通道包括高压氮换热通道和返流的低压氮换热通道，从上游煤气化装置来原料气连接至主换热器中的原料气进口通道，然后其输送管路由主换热器中部抽出，经管路连接至使其进一步冷却的再沸器，再沸器出口由管路连至主换热器中冷却用的原料气换热通道，然后原料气换热通道由管路连接至洗涤塔；主换热器中混合冷剂通道的进出口分别连至闭式混合冷剂循环，其进口端连接混合冷剂压缩机末级出口的分离器，其中分离器的液相输出管经冷剂泵加压连接到进口端，气相输出管直接连至进口端，混合冷剂通道的出口端连接混合冷剂压缩机的吸入口；主换热器中的高压氮换热通道的进口连至氮循环的氮气压缩机末级冷却器的出口，返流的低压氮换热通道的出口连至氮循环的氮气压缩机的进口；洗涤塔顶引出的主要组分为H2和CO的合成气的管路连接至主换热器中返流的合成气通道然后连接至合成气输出管网，洗涤塔底引出的主要组分为H2和CO的液体的管路连接至CH4－CO精馏塔。
本实用新型的附加技术方案如下。 
优选地，氮循环中包括循环氮气压缩机，其增压并冷却后的氮气输出管连接主换热器中的高压氮换热通道，主换热器的氮出口连接至J/T阀，经过J/T阀后连接至CH4－CO精馏塔的冷凝器，冷凝器的氮出口连接至主换热器中的低压氮通道，低压氮通道的输出端连接至循环氮气压缩机入口进行下一次循环。。
优选地，如果采用氮气膨胀的方案则氮循环中还包括增压透平膨胀机，循环氮气压缩机的增压、冷却输出端连接至增压透平膨胀机的增压端，增压透平膨胀机的输出端连接至主换热器中的高压氮换热通道，高压氮换热通道上有管路连接至氮气膨胀机，氮气膨胀机的输出端连接至板式主换热器的低压氮换热通道，主换热器中的高压氮换热通道出主换热器后连接至J/T阀，然后经过J/T阀连接至CH4－CO精馏塔的冷凝器，CH4－CO精馏塔的冷凝器的输出的连接至主换热器中的低压氮换热通道，低压氮换热通道的输出端连接至循环氮气压缩机入口进行下一次循环。 
优选地，所述的闭式混合冷剂循环包括混合冷剂压缩机，压缩后的混合冷剂输出管连接至末级冷却器后的第一汽液分离罐，第一汽液分离罐分离出的混合冷剂液体输出管连接混合冷剂泵加压后连接至主换热器中的混合冷剂换热通道，分离出的混合冷剂气体输出管直接连接主换热器中的混合冷剂换热通道，在换热器内部入口处有使混合冷剂汽液均匀混合的分配结构，该分配结构输出管连至主换热器的每个隔层，然后引出至混合冷剂J/T阀，再连至第二汽液分离罐，汽、液管路分别连至主换热器中不同的通道，在经过换热器内部入口处的分配结构后，连接至主换热器的每个隔层，然后连至混合冷剂压缩机的入口进行下一次循环。 
优选地，在闭式混合冷剂循环中有补充混合冷剂的入口。
优选地，在氮循环中有氮气补充口，氮气补充口接到循环氮气压缩机（NC601）入口管上并与空气分离设备的氮气输出管道连接。 
优选地，在氮循环中有液氮补充口，液氮补充口接到冷凝器(K601)的液氮进口管上并与空气分离设备的液氮输出管道连接。 
本实用新型的有益效果：由于采用闭式混合冷剂制冷循环和氮气制冷循环组合的方式，同时利用空分补充液氮的方法。这样改善主换热器的传热温差，减少主换热器的不可逆损耗，降低整套深冷分离装置的能耗。在氮循环系统用节流阀代替膨胀机时，分离液化LNG的单位能耗仅为：0.7Kw.h/Nm3.LNG，整套系统的可靠性高，操作更加简便,启停更加方便。在氮循环系统用氮气膨胀机时，其分离液化LNG的单位能耗仅为：0.67Kw.h/Nm3.LNG。与无膨胀机的氮循环流程相比，能耗更低。 
附图说明
本实用新型将通过例子并参照附图的方式说明，其中： 
图1是本实用新型煤气化装置来原料气的CH4深冷分离装置的换热系统实施例1的系统框图。
图2是本实用新型煤气化装置来原料气的CH4深冷分离装置的换热系统实施例2的系统框图。 
具体实施方式
下面结合附图和实施例对本实用新型进一步说明。 
本实用新型的具体实施例1，如图1所示，一种煤气化装置来原料气的CH4深冷分离装置的换热系统，包括有板翅式主换热器（E601）、闭式混合冷剂循环压缩机（MRC701）及氮气循环压缩机(NC601)，其中，从上游煤气化装置来原料气连接至主换热器中的原料气进口通道并在其中冷却然后从主换热器中部抽出，经过再沸器（K602）进一步冷却后再进入主换热器中的原料气换热通道冷却并部分冷凝到-165℃～-160℃引出进入洗涤塔（T601）；主换热器中混合冷剂换热通道的进出口分别连至闭式混合冷剂循环，其进口端连接混合冷剂压缩机（MRC701）末级出口的分离器（液相经冷剂泵（P701）加压进入到进口端，气相直接连至进口端），出口端连接混合冷剂压缩机（MRC701）的吸入口；主换热器中的高压氮换热通道的进口连至氮循环的氮气压缩机（NC601）末级冷却器的出口，返流的低压氮换热通道的出口连至氮循环的氮气压缩机（NC601）的进口。洗涤塔（T601）顶引出的合成气（主要是H2和CO）经过主换热器中返流的合成气通道复热后至合成气输出管网，洗涤塔（T601）底引出的CH4－CO混合气引出至CH4－CO精馏塔（T602）。 
其中，主要的制冷负荷由闭式混合冷剂制冷循环提供，将进料原料气冷却至-151℃左右，并且将氮气冷剂冷凝至-151℃左右。冷剂由冷剂压缩机压缩，在换热器中冷却并冷凝，通过混合冷剂节流阀（J/T阀）膨胀以及在换热器E601内复热从而提供冷量。冷剂是由氮气、和C1至C5的碳氢化合物组成的混合物。 
氮循环中，氮气经循环氮气压缩机（NC601）增压并冷却后进入主换热器中的高压氮换热通道，氮气在其中冷却、液化并过冷后出主换热器，进J/T阀，液氮经过J/T阀后进入CH4－CO精馏塔（T602）的冷凝器(K601)，然后进入主换热器中的低压氮通道复热出冷箱汇入循环氮气压缩机（NC601）入口进行下一次循环。液氮为CH4－CO精馏塔T602回流冷凝器K601提供充分的冷量同时返流氮气也将原料气从-151℃进一步冷却到-165℃－-160℃。如果利用空分的液氮给冷凝器K601提供部分冷量同时在主换热器E601复热，可以进一步降低能耗。 
上述实施例的工作流程如下：经净化处理的原料气在主换热器E601中冷却到-165℃－-160℃；混合冷剂从主换热器E601中复热出来（压力2～4bar）与冷剂补充系统来的冷剂混合后进混合冷剂压缩机压缩后（压力～40Bar），再经冷却器WE701冷却进汽液分离罐V701（如果压缩机段间有冷却器则需增设段间汽液分离罐和段间冷剂液体泵），分离后的气相进主换热器E601，液相进冷剂泵P701加压后进主换热器，汽、液分别从不同的通道进入主换热器E601在换热器内部入口处一个特殊分配结构中使汽液均匀混合后，进入主换热器的每个隔层；汽液混合后的冷剂在主换热器E601内冷却液化并过冷到-151℃通过混合冷剂J/T阀节流膨胀到2～4bar，在经过汽液分离罐（V702），混合后返回到主换热器E601复热到进行下一个循环；氮气从主换热器E601中复热出来（压力5～6bar）与空气分离设备中的空分下塔来的补充压力氮气混合后进氮气压缩机NC601压缩冷却后到压力～40Bar，进主换热器E601与返流气换热，氮气在换热器内冷却液化并过冷到-165℃－-160℃，经第一节流阀后节流压力变为5～6bar，进冷凝器K601蒸发后进主换热器复热出冷箱进行下一个循环；可以采用从空气分离装置中补充液氮（液氮流量可以根据空分的液体产量来调节）进冷凝器K601蒸发后进主换热器E601复热出冷箱并入氮气制冷循环的氮气压缩机NC601入口。 
本实用新型的具体实施例2，如图2所示，一种煤气化装置来原料气的CH4深冷分离装置的换热系统，包括有板翅式主换热器（E601）、闭式混合冷剂循环压缩机（MRC701）及氮气循环压缩机(NC601)，如果采用氮气膨胀则还有氮气增压透平膨胀机(ET601)，主换热器E601中布置有原料气换热通道、混合冷剂换热通道和氮换热通道，其中，原料气换热部分和混合冷剂换热部分与实施例1中相同，不同在于氮循环中增加了增压透平膨胀机ET601，氮循环包括氮气经循环氮气压缩机（NC601）增压并冷却后并经膨胀机的增压端增压后进入主换热器中的高压氮换热通道，氮气冷却到一定温度大部分抽出进入氮气膨胀机，膨胀后的氮气进入板式的低压氮换热通道，一小部分氮气在继续冷却、液化并过冷后出主换热器，经J/T阀，液氮经过J/T阀后进入CH4－CO精馏塔（T602）的冷凝器(K601)，然后进入主换热器中的低压氮换热通道复热出冷箱汇入循环氮气压缩机（NC601）入口进行下一次循环。 
本实施例的工作循环和流程与实施例1类似，不同仅在氮循环中增加了膨胀机，在该流程中氮气从主换热器E601中复热出来（压力5～6bar）与空分下塔来的补充压力氮气混合后进氮气压缩机NC601压缩冷却后到压力～27Bar，进增压透平膨胀机ET601增压后进主换热器E601与返流氮气换热，氮气在换热器内冷却到大约-110℃，大部分氮气进膨胀机，膨胀到5～6bar，其余氮气在主换热器内液化并过冷到（-160℃～-165℃）流出，经J/T阀后节流（压力5～6bar）进冷凝器K601蒸发后与膨胀后氮气汇合后进主换热器E601复热出冷箱进行下一个循环。 
本说明书中公开的所有特征，或公开的所有方法或过程中的步骤，除了互相排斥的特征和/或步骤以外，均可以以任何方式组合。 
本说明书（包括任何附加权利要求、摘要和附图）中公开的任一特征，除非特别叙述，均可被其他等效或具有类似目的的替代特征加以替换。即，除非特别叙述，每个特征只是一系列等效或类似特征中的一个例子而已。 
以上所述仅为本实用新型的较佳实施例而已，并不用以限制本实用新型，凡在本实用新型的精神和原则之内所作的任何修改、等同替换和改进等，均应包含在本实用新型的保护范围之内。 

Claims (7)

1.一种煤气化装置来原料气甲烷深冷分离装置的换热系统，包括有板翅式主换热器、闭式混合冷剂循环压缩机及氮气循环压缩机，主换热器中布置有原料气通道、混合冷剂通道和氮气通道，其中，主换热器中的原料气通道包括原料气进口通道、原料气换热通道和返流的合成气通道，氮气通道包括高压氮换热通道和返流的低压氮换热通道，从上游煤气化装置来原料气连接至主换热器中的原料气进口通道，然后其输送管路由主换热器中部抽出，经管路连接至使其进一步冷却的再沸器，再沸器出口由管路连至主换热器中冷却用的原料气换热通道，然后原料气换热通道由管路连接至洗涤塔；主换热器中混合冷剂通道的进出口分别连至闭式混合冷剂循环，其进口端连接混合冷剂压缩机末级出口的分离器，其中分离器的液相输出管经冷剂泵加压连接到进口端，气相输出管直接连至进口端，混合冷剂通道的出口端连接混合冷剂压缩机的吸入口；主换热器中的高压氮换热通道的进口连至氮循环的氮气压缩机末级冷却器的出口，返流的低压氮换热通道的出口连至氮循环的氮气压缩机的进口；洗涤塔顶引出的主要组分为H2和CO的合成气的管路连接至主换热器中返流的合成气通道然后连接至合成气输出管网，洗涤塔底引出的主要组分为H2和CO的液体的管路连接至CH4－CO精馏塔。
2.根据权利要求1所述的煤气化装置来原料气甲烷深冷分离装置的换热系统，其特征在于，所述的闭式混合冷剂循环包括混合冷剂压缩机，压缩后的混合冷剂输出管连接至末级冷却器后的第一汽液分离罐，第一汽液分离罐分离出的混合冷剂液体输出管连接混合冷剂泵加压后连接至主换热器中的混合冷剂换热通道，分离出的混合冷剂气体输出管直接连接主换热器中的混合冷剂换热通道，在换热器内部入口处有使混合冷剂汽液均匀混合的分配结构，该分配结构输出管连至主换热器的每个隔层，然后引出至混合冷剂J/T阀，再连至第二汽液分离罐，汽、液管路分别连至主换热器中不同的通道，在经过换热器内部入口处的分配结构后，连接至主换热器的每个隔层，然后连至混合冷剂压缩机的入口进行下一次循环。
3.根据权利要求1所述的煤气化装置来原料气甲烷深冷分离装置的换热系统，其特征在于，氮循环中包括循环氮气压缩机，其增压并冷却后的氮气输出管连接主换热器中的高压氮换热通道，主换热器的氮出口连接至J/T阀，经过J/T阀后连接至CH4－CO精馏塔的冷凝器，冷凝器的氮出口连接至主换热器中的低压氮通道，低压氮通道的输出端连接至循环氮气压缩机入口进行下一次循环。
4.根据权利要求1所述的煤气化装置来原料气甲烷深冷分离装置的换热系统，其特征在于，氮循环中还包括增压透平膨胀机和循环氮气压缩机，循环氮气压缩机的增压、冷却输出端连接至增压透平膨胀机的增压端，增压透平膨胀机的输出端连接至主换热器中的高压氮换热通道，高压氮换热通道上有管路连接至氮气膨胀机，氮气膨胀机的输出端连接至板式主换热器的低压氮换热通道，主换热器中的高压氮换热通道出主换热器后连接至J/T阀，然后经过J/T阀连接至CH4－CO精馏塔的冷凝器，CH4－CO精馏塔的冷凝器的输出的连接至主换热器中的低压氮换热通道，低压氮换热通道的输出端连接至循环氮气压缩机入口进行下一次循环。
5.根据权利要求2所述的煤气化装置来原料气甲烷深冷分离装置的换热系统，其特征在于，在混合冷剂循环中有补充混合冷剂的入口。
6.根据权利要求3所述的煤气化装置来原料气甲烷深冷分离装置的换热系统，其特征在于，在氮循环中有氮气补充口，氮气补充口接到循环氮气压缩机入口管上并与空气分离设备的氮气输出管道连接。
7.根据权利要求3所述的煤气化装置来原料气甲烷深冷分离装置的换热系统，其特征在于，在氮循环中有液氮补充口，液氮补充口接到冷凝器的液氮进口管上并与空气分离设备的液氮输出管道连接。
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101782308A (zh) * 2009-08-26 2010-07-21 成都蜀远煤基能源科技有限公司 煤气化装置来原料气甲烷深冷分离装置的换热系统
CN103277978A (zh) * 2013-06-08 2013-09-04 中国科学院理化技术研究所 提取低浓度含氧煤层气中甲烷的装置

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101782308A (zh) * 2009-08-26 2010-07-21 成都蜀远煤基能源科技有限公司 煤气化装置来原料气甲烷深冷分离装置的换热系统
CN103277978A (zh) * 2013-06-08 2013-09-04 中国科学院理化技术研究所 提取低浓度含氧煤层气中甲烷的装置
CN103277978B (zh) * 2013-06-08 2015-07-15 中国科学院理化技术研究所 提取低浓度含氧煤层气中甲烷的装置

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