CN101608859B - 高低压氮气双膨胀天然气液化方法 - Google Patents
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Abstract
本发明公开了一种高低压氮气双膨胀天然气液化方法,包括如下步骤,氮气被压缩,冷却后进入低压增压机的增压端增压,经第二后冷却器冷却到30~45℃,再进入高压增压机的增压端,得到高压氮气,高压氮气经第一后冷却器冷却得到30~45℃;被冷却后的高压氮气进入主换热器与原料天然气被低压膨胀机出口的低压氮气冷却冷却到-70~-30℃后抽出一股,送入高压膨胀机膨胀制冷后,再进入低压膨胀机膨胀制冷,得到低压氮气,同时原料天然气被低压氮气继续冷却、液化、过冷后出主换热器;出主换热器的原料天然气经节流阀节流,分离灌分离后,得到液态天然气送入贮槽,气体返回主换热器回收冷量。本发明适用于高低压区,且液化率高,可达100%。
Description
技术领域
本发明涉及一种天然气液化方法,尤其涉及一种高低压氮气双膨胀天然气液化方法。
背景技术
随着社会的发展,石油储存量在减少,温室效应越来越明显;人们对绿色能源的要求也愈来愈强烈,于是天然气得到了广泛应用。但是天然气开采出来的均为气态,几乎不可能运输,这样就大大地制约了它使用。天然气的液化比为591,如果把天然气液化,体积缩小591倍,运输就成为可能,所以就出现了大量的天然气液化装置。天然气的液化工艺主要有氮膨胀制冷流程、氮-甲烷膨胀制冷流程、混合工质制冷流程等。
其中氮膨胀制冷流程又根据用户的产量及压力不同分为:氮气单膨胀制冷流程(主要用于产量小于30吨/天),冷冻机加氮气单膨胀制冷流程(主要用于产量为30~100吨/天),氮气双膨胀制流程(主要用于产量为100~600吨/天)冷。但是还没有用高低压氮气膨胀制冷液化流程,这里主要介绍高低压氮气双膨胀天然气液化流程,此流程为氮气双膨胀制流程的一种。
发明内容
本发明的目的是提供一种高低压氮气双膨胀天然气液化方法,解决了现有技术中存在的问题。
本发明所采用的技术方案是,高低压氮气双膨胀天然气液化方法,其特征在于包括如下步骤:
a、氮气被压缩到2.0~3.0MPa,冷却到30~45℃;
b、步骤a得到的氮气进入低压增压机的增压端增压后,经第二后冷却器冷却到30~45℃,再进入高压增压机的增压端,得到3.6~5.3MPa高压氮气,高压氮气经第一后冷却器冷却到30~45℃;
c、被冷却后的高压氮气进入主换热器与原料天然气被低压膨胀机出口的0.4~0.6MPa低压氮气冷却冷却到-70~-30℃后抽出一股,送入高压膨胀机膨胀制冷后,再进入低压膨胀机膨胀制冷,得到0.4~0.6MPa低压氮气,同时原料天然气被低压氮气继续冷却、液化、过冷后出主换热器;
d、出主换热器的原料天然气经节流阀节流,分离灌分离后,得到液态天然气送入贮槽,气体返回主换热器回收冷量。
由于本发明提供的方法采用高压增压机和低压增压机增压,高压膨胀机和低压膨胀机膨胀制冷,所液化效果更好。且液化率高,可达100%。
附图说明
图1是本发明的原理示意图。
具体实施方式
下面结合附图和具体实施方式对本发明进行详细说明。
本发明提供一种高低压氮气双膨胀天然气液化方法,包括如下步骤
a、氮气被压缩到2.0~3.0MPa,冷却到30~45℃;
b、步骤a得到的氮气进入低压增压机2的增压端增压后,经第二后冷却器4冷却到30~45℃,再进入高压增压机1的增压端,得到3.6~5.3MPa高压氮气,高压氮气经第一后冷却器3冷却到30~45℃;
c、被冷却后的高压氮气进入主换热器9与1.0MPa~10Mpa原料天然气被低压膨胀机6出口的0.4~0.6MPa低压氮气冷却冷却到-70~-30℃后抽出一股,送入高压膨胀机5,高压膨胀机5在高压4.0MPa高温-50℃下膨胀制冷,膨胀比为2~3,再进入低压膨胀机6,低压膨胀机6在高压1.8MPa低温-90℃下膨胀制冷,膨胀比为3~6,同时1.0MPa~10Mpa原料天然气被0.4~0.6MPa低压氮气继续冷却、液化、过冷后出主换热器;
d、出主换热器的原料天然气经节流阀7节流,分离灌8分离后,得到压力为0.3MPa~0.7Mpa的液态天然气送入贮槽,气体返回主换热器回收冷量。
实施例1
高低压氮气双膨胀天然气液化方法,包括如下步骤:
a、氮气被压缩到2.0MPa,冷却到30℃;
b、步骤a得到的氮气进入低压增压机2的增压端增压后,经第二后冷却器4冷却到30℃,再进入高压增压机1的增压端,得到3.6MPa高压氮气,3.6MPa高压氮气经第一后冷却器3冷却到30℃;
c、被冷却后的高压氮气进入主换热器9与1.0MPaMpa原料天然气被低压膨胀机6出口的0.4MPa低压氮气冷却冷却到-30℃后抽出一股,送入高压膨胀机5,高压膨胀机5在高压4.0MPa高温-50℃下膨胀制冷,膨胀比为2,再进入低压膨胀机6,低压膨胀机6在高压1.8MPa低温-90℃下膨胀、制冷,膨胀比为3,同时1.0Mpa原料天然气被0.4MPa低压氮气继续冷却、液化、过冷后出主换热器;
d、出主换热器的原料天然气经节流阀7节流,分离灌8分离后,得到压力为0.3MPa的液态天然气送入贮槽,气体返回主换热器回收冷量。
实施例2
高低压氮气双膨胀天然气液化方法,包括如下步骤:
a、氮气被压缩到3.0MPa,冷却到45℃;
b、步骤a得到的氮气进入低压增压机2的增压端增压后,经第二后冷却器4冷却到45℃,再进入高压增压机1的增压端,得到5.3MPa高压氮气,5.3MPa高压氮气经第一后冷却器3冷却到45℃;
c、被冷却后的高压氮气进入主换热器9与1.0MPa~10Mpa原料天然气被低压膨胀机6出口的0.6MPa低压氮气冷却冷却到-70℃后抽出一股,送入高压膨胀机5,高压膨胀机5在高压4.0MPa高温-50℃下膨胀制冷,膨胀比为3,再进入低压膨胀机6,低压膨胀机6在高压1.8MPa低温-90℃下膨胀制冷,膨胀比为6,同时10Mpa原料天然气被0.6MPa低压氮气继续冷却、液化、过冷后出主换热器;
d、出主换热器的原料天然气经节流阀7节流,分离灌8分离后,得到压力为0.7Mpa的液态天然气送入贮槽,气体返回主换热器回收冷量。
实施例3
高低压氮气双膨胀天然气液化方法,包括如下步骤:
a、氮气被压缩到2.5MPa,冷却到35℃;
b、步骤a得到的氮气进入低压增压机2的增压端增压后,经第二后冷却器4冷却到35℃,再进入高压增压机1的增压端,得到4.0MPa高压氮气,4.0MPa高压氮气经第一后冷却器3冷却到35℃;
c、被冷却后的高压氮气进入主换热器9与1.6Mpa原料天然气被低压膨胀机6出口的0.5MPa低压氮气冷却冷却到-40℃后抽出一股,送入高压膨胀机5,高压膨胀机5在高压4.0MPa高温-50℃下膨胀制冷,膨胀比为2.5,再进入低压膨胀机6,低压膨胀机6在高压1.8MPa低温-90℃下膨胀制冷,膨胀比为4,同时1.6Mpa原料天然气被0.5MPa低压氮气继续冷却、液化、过冷后出主换热器;
d、出主换热器的原料天然气经节流阀7节流,分离灌8分离后,得到压力为0.4Mpa的液态天然气送入贮槽,气体返回主换热器回收冷量。
实施例4
高低压氮气双膨胀天然气液化方法,包括如下步骤:
a、氮气被压缩到2.2MPa,冷却到40℃;
b、步骤a得到的氮气进入低压增压机2的增压端增压后,经第二后冷却器4冷却到40℃,再进入高压增压机1的增压端,得到5.0MPa高压氮气,5.0MPa高压氮气经第一后冷却器3冷却得到40℃;
c、被冷却后的高压氮气进入主换热器9与5.0Mpa原料天然气被低压膨胀机6出口的0.55MPa低压氮气冷却冷却到-50℃后抽出一股,送入高压膨胀机5,高压膨胀机5在高压4.0MPa高温-50℃下膨胀制冷,膨胀比为2.5,再进入低压膨胀机6,低压膨胀机6在高压1.8MPa低温-90℃下膨胀制冷,膨胀比为5,同时5Mpa原料天然气被0.55MPa低压氮气继续冷却、液化、过冷后出主换热器;
d、出主换热器的原料天然气经节流阀7节流,分离灌8分离后,得到压力为0.6Mpa的液态天然气送入贮槽,气体返回主换热器回收冷量。
Claims (5)
1.高低压氮气双膨胀天然气液化方法,其特征在于包括如下步骤:
a、氮气被压缩到2.0~3.0MPa,冷却到30~45℃;
b、步骤a得到的氮气进入低压增压机(2)的增压端增压后,经第二后冷却器(4)冷却到30~45℃,再进入高压增压机(1)的增压端,得到3.6~5.3MPa高压氮气,高压氮气经第一后冷却器(3)冷却到30~45℃;
c、被冷却后的高压氮气进入主换热器(9)与原料天然气被低压膨胀机(6)出口的0.4~0.6MPa低压氮气冷却到-70~-30℃后抽出一股,送入高压膨胀机(5)膨胀制冷后,再进入低压膨胀机(6)膨胀制冷,得到0.4~0.6MPa低压氮气,同时原料天然气被0.4~0.6MPa低压氮气继续冷却、液化、过冷后出主换热器;
d、出主换热器的原料天然气经节流阀(7)节流,分离罐(8)分离后,得到液态天然气送入贮槽,气体返回主换热器回收冷量。
2.根据权利要求1所述的高低压氮气双膨胀天然气液化方法,其特征在于,所述高压膨胀机(5)在高压4.0MPa高温-50℃下膨胀,膨胀比为2~3,低压膨胀机(6)在高压1.8MPa低温-90℃下膨胀,膨胀比为3~6。
3.根据权利要求1所述的高低压氮气双膨胀天然气液化方法,其特征在于,原料天然气的压力为1.0MPa~10Mpa。
4.根据权利要求3所述的高低压氮气双膨胀天然气液化方法,其特征在于,原料天然气的压力为1.6MPa~5Mpa。
5.根据权利要求1所述的高低压氮气双膨胀天然气液化方法,其特征在于,液态天然气压力为0.3MPa~0.7Mpa。
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CN102504901A (zh) * | 2011-11-03 | 2012-06-20 | 苏州市兴鲁空分设备科技发展有限公司 | 天然气液化方法 |
CN104101177A (zh) * | 2014-07-31 | 2014-10-15 | 银川天佳能源科技股份有限公司 | 用于天然气液化的卧式冷箱 |
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Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN1016267B (zh) * | 1988-09-06 | 1992-04-15 | 气体产品与化学公司 | 液化天然气蒸发气体的再液化流程 |
CN1107571A (zh) * | 1993-12-31 | 1995-08-30 | 乔治·克劳德方法的研究开发空气股份有限公司 | 液化气体用的工艺和成套设备 |
CN1310322A (zh) * | 2000-01-10 | 2001-08-29 | 普莱克斯技术有限公司 | 工业气体低温液化系统 |
US6446465B1 (en) * | 1997-12-11 | 2002-09-10 | Bhp Petroleum Pty, Ltd. | Liquefaction process and apparatus |
CN101008545A (zh) * | 2007-01-24 | 2007-08-01 | 河南中原绿能高科有限责任公司 | 一种用于天然气液化的新型ⅱ阶混合制冷工艺 |
CN101137878A (zh) * | 2005-03-14 | 2008-03-05 | 海威Kse气体系统公司 | 冷却汽化气体流的系统和方法 |
CN101180509A (zh) * | 2005-04-11 | 2008-05-14 | 泰克尼普法国公司 | 将利用第一冷却循环冷却所获gnl流过冷的方法及相关设备 |
-
2008
- 2008-06-20 CN CN200810062538XA patent/CN101608859B/zh active Active
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN1016267B (zh) * | 1988-09-06 | 1992-04-15 | 气体产品与化学公司 | 液化天然气蒸发气体的再液化流程 |
CN1107571A (zh) * | 1993-12-31 | 1995-08-30 | 乔治·克劳德方法的研究开发空气股份有限公司 | 液化气体用的工艺和成套设备 |
US6446465B1 (en) * | 1997-12-11 | 2002-09-10 | Bhp Petroleum Pty, Ltd. | Liquefaction process and apparatus |
CN1310322A (zh) * | 2000-01-10 | 2001-08-29 | 普莱克斯技术有限公司 | 工业气体低温液化系统 |
CN101137878A (zh) * | 2005-03-14 | 2008-03-05 | 海威Kse气体系统公司 | 冷却汽化气体流的系统和方法 |
CN101180509A (zh) * | 2005-04-11 | 2008-05-14 | 泰克尼普法国公司 | 将利用第一冷却循环冷却所获gnl流过冷的方法及相关设备 |
CN101008545A (zh) * | 2007-01-24 | 2007-08-01 | 河南中原绿能高科有限责任公司 | 一种用于天然气液化的新型ⅱ阶混合制冷工艺 |
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