CN102374754B - 从焦炉煤气中制取液态天然气及一氧化碳的设备及方法 - Google Patents

从焦炉煤气中制取液态天然气及一氧化碳的设备及方法 Download PDF

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CN102374754B
CN102374754B CN201110286175.XA CN201110286175A CN102374754B CN 102374754 B CN102374754 B CN 102374754B CN 201110286175 A CN201110286175 A CN 201110286175A CN 102374754 B CN102374754 B CN 102374754B
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heat exchanger
nitrogen
main heat
tower
pressure
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赵德泉
杨光达
于艳君
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Liaoning CIMC Hashenleng Gas Liquefaction Equipment Co Ltd
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LIAONING HARBIN SHENLENG GAS LIQUEFACTION EQUIPMENT CO Ltd
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    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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Abstract

本发明涉及一种从焦炉煤气中制取液态天然气及一氧化碳的设备及方法。传统的低温液化系统流程过长投资大且一氧化碳纯度低。本发明的组成包括：冷箱中的主换热器（1），主换热器分别连接混合制冷剂压缩制冷系统及氮气压缩制冷系统；主换热器经管路连接高压精馏塔（2），高压精馏塔的塔底具有再沸器（3），再沸器经管路连接所述的主换热器后连接液化天然气贮槽（4）；高压精馏塔顺次连接主冷凝蒸发器（5）和低压精馏塔（6），所述的主冷凝蒸发器连接分离器（7）及其气体输出管路（8）；所述的低压精馏塔经管路连接冷凝器（9），所述的冷凝器输出管路经过过冷器（10）连接到所述的主换热器后连接到尾气输出管路（11）。本发明用于从焦炉煤气中制取液态天然气及一氧化碳。

Description

从焦炉煤气中制取液态天然气及一氧化碳的设备及方法
技术领域：
本发明涉及一种从焦炉煤气中制取液态天然气及一氧化碳的设备及方法。
背景技术：
焦炉煤气又称炼焦煤气，其主要成分为含量55%左右的氢气、含量约25%左右的甲烷(CH4)、一氧化碳(CO)、二氧化碳(CO2)和氮气（N2）的含量约20%。由于焦炉气富含氢气、甲烷与一氧化碳，焦炉气综合利用有二种方法，其一是：可通过甲烷化反应来提高热值，使绝大部分一氧化碳、二氧化碳转化成甲烷，可以得到甲烷体积分数40-50%以上的合成天然气，再经液化得到液化天然气（LNG）；其二是：将焦炉煤气中甲烷提取后，联产一氧化碳气体，再将氢气与一氧化碳合成甲醇。焦炉煤气生产液化天然气联产甲醇装置，具有投资小，消耗低，无污染、能量利用率高、产品市场前景好等优势，是焦化企业煤气利用的较佳选择。
焦炉煤气生产液化天然气联产甲醇装置，其设计难点在于既要低能耗生产LNG，又要兼顾提取较高纯度一氧化碳用于合成甲醇。一氧化碳中的氮气、甲烷等杂质对于合成甲醇来说属于惰性气体，其存在将抑制甲醇合成反应增加能耗。而一氧化碳与氮气常压下沸点很接近分离功耗高。传统方法低温液化系统仅考虑生产LNG,富含氢气、一氧化碳的尾气出冷箱后采用非低温方法如PSA法或膜分离法生产一氧化碳，不但流程过长投资大且一氧化碳纯度低。
发明内容：
本发明的目的是提出一种可靠性好、效率高、运行费用低的从焦炉煤气中制取液态天然气及一氧化碳的设备及方法。
上述的目的通过以下的技术方案实现：
一种从焦炉煤气中制取液态天然气及一氧化碳的设备，其组成包括：冷箱中的主换热器，主换热器分别连接混合制冷剂压缩制冷系统及氮气压缩制冷系统；主换热器经管路连接高压精馏塔，高压精馏塔的塔底具有再沸器，再沸器经管路连接所述的主换热器后连接液化天然气贮槽；高压精馏塔顺次连接主冷凝蒸发器和低压精馏塔，所述的主冷凝蒸发器连接分离器及其气体输出管路；所述的低压精馏塔经管路连接冷凝器，所述的冷凝器输出管路经过过冷器连接到所述的主换热器后连接到尾气输出管路；所述的混合制冷剂压缩制冷系统包括混合制冷剂压缩机，所述的混合制冷剂压缩机通过混合制冷剂管道连接所述的主换热器，从所述的主换热器的中部抽出的混合制冷剂的管路连接所述的再沸器，从所述的再沸器输出的所述的混合制冷剂的管路通过管道连接所述的主换热器，最后复热后的介质管道连接所述的混合制冷剂压缩机形成循环；所述的氮气压缩制冷系统包括氮气压缩机，所述的氮气压缩机将氮气压缩后通过管道连接所述的主换热器，冷却后的氮气管路经节流阀连接到所述的冷凝器，从所述的冷凝器输出的氮气的管道连接所述的过冷器，从所述的过冷器输出的介质管道连接所述的氮气压缩机形成循环。
所述的设备从焦炉煤气中制取液态天然气及一氧化碳的方法，该方法包括如下过程：净化后的焦炉煤气进入主换热器被返流的低温介质冷却到-150℃~-170℃进入高压精馏塔中部进行精馏，高压精馏塔塔釜获得LNG经主换热器过冷后经节流阀减压送至液化天然气贮槽中储存；高压精馏塔塔顶部抽出富含氢气、氮气、及一氧化碳的汽液混合物经分离器分离后，气相经主换热器复热后送出，液态中一部分经过冷器被过冷经节流阀减压后，进入低压精馏塔中部参加精馏；另一部分液体靠重力回流到高压精馏塔顶部作为高压精馏塔回流液，低压精馏塔底部获得液态一氧化碳在主冷凝蒸发器被高压精馏塔顶部氢-氮气-一氧化碳气体加热气化后抽出，后经主换热器复热后送出，低压精馏塔塔顶部气体进入冷凝器被液氮冷凝后成为汽液混合物，液态物质靠重力返回低压精馏塔顶部作为回流液，气体尾气与塔顶冷凝器蒸发的氮气进入过冷器去冷却来自高压精馏塔顶部分离器的氮-氢-一氧化碳混合液体，尾气经主换热器复热送出，混合制冷剂在主换热器中部抽出，进入高压精馏塔底部再沸器作为热源加热塔底部LNG，高压制冷剂冷却后回到主换热器，继续冷却到过冷液体后经节流阀减压降温后，冷却主换热器各热流体被复热后出冷箱进入混合制冷剂压缩机循环压缩，氮气经氮气压缩机压缩后，进入主换热器中部冷却为过冷液体后，通过节流阀减压，为低压精馏塔顶部冷凝器提供冷源，被加热蒸发后再经过冷器过热后循环压缩。
所述的从焦炉煤气中制取液态天然气及一氧化碳的方法，所述的混合制冷剂压缩制冷系统中所使用的混合制冷剂由甲烷、乙烯、丙烷、异丁烷和氮气混合而成。
所述的从焦炉煤气中制取液态天然气及一氧化碳的方法，所述的氮气压缩制冷系统中中所使用的工质为氮气或者甲烷含量为10%~40%的氮和甲烷的混合气体。
有益效果：
1.本发明将高、低压塔巧妙的用一台冷凝蒸发器耦合起来，高压塔顶部氢-氮气-一氧化碳气体作为热介质通过冷凝蒸发器被低压塔底部液态一氧化碳冷凝，而低压塔底部液态一氧化碳作为冷介质则被蒸发，通过调整高压塔压力及塔顶排出量可方便的调整冷凝温度适应冷凝蒸发器工况。
、本发明流程简单：二只塔就可获得LNG产品及一氧化碳产品。
、能耗低：由于生产LNG是在高压塔完成，适应了甲烷与其它气体沸点相差悬殊易于精馏的特点，原料气压力无损失；高压塔的液体过冷后进入低压塔，节流阀损失小，一氧化碳在低压塔精馏获得，适应了一氧化碳与氮气沸点差别小不易精馏的特点，采用阻力小的高理论塔数规整填料塔可获得高纯度一氧化碳。
附图说明：
附图1是本发明的结构示意图。
具体实施方式：
实施例1：
从焦炉煤气中制取液态天然气及一氧化碳的设备，其组成包括：冷箱中的主换热器1，主换热器分别连接混合制冷剂压缩制冷系统及氮气压缩制冷系统；主换热器经管路连接高压精馏塔2，高压精馏塔的塔底具有再沸器3，再沸器经管路连接所述的主换热器后连接液化天然气贮槽4；高压精馏塔顺次连接主冷凝蒸发器5和低压精馏塔6，所述的主冷凝蒸发器连接分离器7及其气体输出管路8；所述的低压精馏塔经管路连接冷凝器9，所述的冷凝器输出管路经过过冷器10连接到所述的主换热器后连接到尾气输出管路11。
实施例2：
所述的从焦炉煤气中制取液态天然气及一氧化碳的设备，所述的混合制冷剂压缩制冷系统包括混合制冷剂压缩机13，所述的混合制冷剂压缩机通过混合制冷剂管道连接所述的主换热器，从所述的主换热器的中部抽出的混合制冷剂的管路连接所述的再沸器，从所述的再沸器输出的所述的混合制冷剂的管路通过管道连接所述的主换热器，最后复热后的介质管道连接所述的混合制冷剂压缩机形成循环。
实施例3：
所述的从焦炉煤气中制取液态天然气及一氧化碳的设备，所述的氮气压缩制冷系统包括氮气压缩机12，所述的氮气压缩机将氮气压缩后通过管道连接所述的主换热器，冷却后的天气管路经节流阀连接到所述的冷凝器，从所述的冷凝器输出的氮气的管道连接所述的过冷器，从所述的过冷器输出的介质管道连接所述的氮气压缩机形成循环。
实施例4：
利用上述设备从焦炉煤气中制取液态天然气及一氧化碳的方法，该方法包括如下过程：
净化后的焦炉气进入冷箱内的主换热器:被返流的低温介质冷却，在-150℃~-170℃下以接近全液态进入高压塔中部进行精馏，塔釜获得LNG经主换热器冷段过冷后经节流阀减压至贮罐压力送至常压LNG贮罐中储存；塔顶部抽出富含氢气、氮气、及一氧化碳的汽液混合物经分离器分离后，气相经主换热器复热后送出冷箱，可进一步提取氢气或作为燃料。液态中一部分经过冷器被过冷后经节流阀减压后，进入低压精馏塔中部参加精馏；另一部分液体靠重力回流到高压塔顶部作为高压塔回流液。低压塔底部获得液态一氧化碳在主冷凝蒸发器被高压塔顶部氢-氮气-一氧化碳气体加热气化后抽出，经主换热器复热后，送出冷箱作为合成甲醇原料；低压塔塔顶部气体进入冷凝器被液氮冷凝后成为汽液混合物，液态靠重力返回低压塔顶部作为回流液，排出富含氮气、氢气、及少量一氧化碳的尾气，这部分气体与塔顶冷凝器蒸发的氮气进入过冷器，去冷却氮-氢-一氧化碳混合液体，尾气经主换热器复热送出冷箱，混合制冷剂在主换热器中部-70℃~-90℃下抽出，进入高压精馏塔底部再沸器作为热源加热塔低部LNG，高压制冷剂冷却后回到主换热器，继续冷却到157℃的过冷液体，经节流阀减压降温后，冷却主换热器各热流体被复热后出冷箱进入混合制冷剂压缩机循环压缩，氮气经低温氮气压缩机压缩到1.5~2.0MPa，进入主换热器中部冷却为-160℃~--170℃的过冷液体后，通过液氮节流阀减压至0.12MPa，为低压精馏塔顶部冷凝器提供冷源，被加热蒸发后再经过冷器过热后循环压缩。
实施例5：
所述的从焦炉煤气中制取液态天然气及一氧化碳的方法，所述的混合制冷剂压缩制冷系统中所使用的混合制冷剂由甲烷、乙烯、丙烷、异丁烷和氮气混合而成。出冷箱的混合制冷剂在0.28MPa下进入混合制冷剂压缩机，被压缩至3.5MPa并冷却后进入主换热器，混合制冷剂在主换热器中部-70℃~-90℃下抽出，进入高压精馏塔底部再沸器作为热源加热塔低部LNG，高压制冷剂冷却到-95℃~-110℃后回到主换热器，继续冷却到-157℃过冷液体后经节流阀减压至0.33MPa降温后，冷却主换热器各热流体被复热后出冷箱进入混合制冷剂压缩机循环压缩。
实施例6：
所述的从焦炉煤气中制取液态天然气及一氧化碳的方法，所述的氮气压缩制冷系统中中所使用的工质为氮气或者甲烷含量为10%~40%的氮和甲烷的混合气体。氮气经低温氮气压缩机压缩到1.5~2.0MPa后，进入主换热器中部冷却为-160℃~--170℃的过冷液体后，通过液氮节流阀减压至0.12MPa，为低压精馏塔顶部冷凝器提供冷源，被加热蒸发后再经过冷器过热后循环压缩。

Claims (4)

1.一种从焦炉煤气中制取液态天然气及一氧化碳的设备，其组成包括：冷箱中的主换热器，其特征是：主换热器分别连接混合制冷剂压缩制冷系统及氮气压缩制冷系统；主换热器经管路连接高压精馏塔，高压精馏塔的塔底具有再沸器，再沸器经管路连接所述的主换热器后连接液化天然气贮槽；高压精馏塔顺次连接主冷凝蒸发器和低压精馏塔，所述的主冷凝蒸发器连接分离器及其气体输出管路；所述的低压精馏塔经管路连接冷凝器，所述的冷凝器输出管路经过过冷器连接到所述的主换热器后连接到尾气输出管路；所述的混合制冷剂压缩制冷系统包括混合制冷剂压缩机，所述的混合制冷剂压缩机通过混合制冷剂管道连接所述的主换热器，从所述的主换热器的中部抽出的混合制冷剂的管路连接所述的再沸器，从所述的再沸器输出的所述的混合制冷剂的管路通过管道连接所述的主换热器，最后复热后的介质管道连接所述的混合制冷剂压缩机形成循环；所述的氮气压缩制冷系统包括氮气压缩机，所述的氮气压缩机将氮气压缩后通过管道连接所述的主换热器，冷却后的氮气管路经节流阀连接到所述的冷凝器，从所述的冷凝器输出的氮气的管道连接所述的过冷器，从所述的过冷器输出的介质管道连接所述的氮气压缩机形成循环。
2.一种利用权利要求1所述的设备从焦炉煤气中制取液态天然气及一氧化碳的方法，其特征是：该方法包括如下过程：净化后的焦炉煤气进入主换热器被返流的低温介质冷却到-150℃~-170℃进入高压精馏塔中部进行精馏，高压精馏塔塔釜获得LNG经主换热器过冷后经节流阀减压送至液化天然气贮槽中储存；高压精馏塔塔顶部抽出富含氢气、氮气、及一氧化碳的汽液混合物经分离器分离后，气相经主换热器复热后送出，液态中一部分经过冷器被过冷经节流阀减压后，进入低压精馏塔中部参加精馏；另一部分液体靠重力回流到高压精馏塔顶部作为高压精馏塔回流液，低压精馏塔底部获得液态一氧化碳在主冷凝蒸发器被高压精馏塔顶部氢-氮气-一氧化碳气体加热气化后抽出，后经主换热器复热后送出，低压精馏塔塔顶部气体进入冷凝器被液氮冷凝后成为汽液混合物，液态物质靠重力返回低压精馏塔顶部作为回流液，气体尾气与塔顶冷凝器蒸发的氮气进入过冷器去冷却来自高压精馏塔顶部分离器的氮-氢-一氧化碳混合液体，尾气经主换热器复热送出，混合制冷剂在主换热器中部抽出，进入高压精馏塔底部再沸器作为热源加热塔底部LNG，高压制冷剂冷却后回到主换热器，继续冷却到过冷液体后经节流阀减压降温后，冷却主换热器各热流体被复热后出冷箱进入混合制冷剂压缩机循环压缩，氮气经氮气压缩机压缩后，进入主换热器中部冷却为过冷液体后，通过节流阀减压，为低压精馏塔顶部冷凝器提供冷源，被加热蒸发后再经过冷器过热后循环压缩。
3.根据权利要求2所述的从焦炉煤气中制取液态天然气及一氧化碳的方法，其特征是：所述的混合制冷剂压缩制冷系统中所使用的混合制冷剂由甲烷、乙烯、丙烷、异丁烷和氮气混合而成。
4.根据权利要求2或3所述的从焦炉煤气中制取液态天然气及一氧化碳的方法，其特征是：所述的氮气压缩制冷系统中中所使用的工质为氮气或者甲烷含量为10%~40%的氮和甲烷的混合气体。
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Publication number Priority date Publication date Assignee Title
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CN116753675A (zh) * 2023-04-06 2023-09-15 西南石油大学 一种适用于地下煤制气分级提纯与液化的方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5365740A (en) * 1992-07-24 1994-11-22 Chiyoda Corporation Refrigeration system for a natural gas liquefaction process
CN1501044A (zh) * 2002-11-01 2004-06-02 液体空气乔治洛德方法利用和研究的具 组合的空气分离和天然气液化装置
CN201251346Y (zh) * 2007-12-17 2009-06-03 中国科学院理化技术研究所 焦炉煤气制取液化天然气的分离设备
KR20090110964A (ko) * 2008-04-21 2009-10-26 대우조선해양 주식회사 혼합냉매 사이클 및 질소 팽창 사이클을 이용한 천연가스액화방법 및 장치
CN101929788A (zh) * 2010-09-15 2010-12-29 中国科学院理化技术研究所 含氧煤层气制取液化天然气的装置
CN201844655U (zh) * 2010-09-15 2011-05-25 煤炭科学研究总院重庆研究院 含氧煤层气液化分离装置
CN202267322U (zh) * 2011-09-24 2012-06-06 辽宁哈深冷气体液化设备有限公司 从焦炉煤气中制取液态天然气及一氧化碳的设备

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5365740A (en) * 1992-07-24 1994-11-22 Chiyoda Corporation Refrigeration system for a natural gas liquefaction process
CN1501044A (zh) * 2002-11-01 2004-06-02 液体空气乔治洛德方法利用和研究的具 组合的空气分离和天然气液化装置
CN201251346Y (zh) * 2007-12-17 2009-06-03 中国科学院理化技术研究所 焦炉煤气制取液化天然气的分离设备
KR20090110964A (ko) * 2008-04-21 2009-10-26 대우조선해양 주식회사 혼합냉매 사이클 및 질소 팽창 사이클을 이용한 천연가스액화방법 및 장치
CN101929788A (zh) * 2010-09-15 2010-12-29 中国科学院理化技术研究所 含氧煤层气制取液化天然气的装置
CN201844655U (zh) * 2010-09-15 2011-05-25 煤炭科学研究总院重庆研究院 含氧煤层气液化分离装置
CN202267322U (zh) * 2011-09-24 2012-06-06 辽宁哈深冷气体液化设备有限公司 从焦炉煤气中制取液态天然气及一氧化碳的设备

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