CN85108285A - 从天然气中分离c2+烃馏分的方法 - Google Patents

从天然气中分离c2+烃馏分的方法 Download PDF

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CN85108285A
CN85108285A CN85108285.8A CN85108285A CN85108285A CN 85108285 A CN85108285 A CN 85108285A CN 85108285 A CN85108285 A CN 85108285A CN 85108285 A CN85108285 A CN 85108285A
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保罗·库曼
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Abstract

提出一种借助于精馏从高压下的天然气中分离C2+烃的方法。精馏所要求的温度和压力值，通过热交换和两级有效降压取得，其中精馏在两个降压段之间进行。精馏所得的甲烷馏分首先被加热至环境温度，然后有效降压并重新加热至环境温度。精馏的塔顶冷却主要通过待分解天然气的有效降压取得。

Description

本发明涉及借助于精馏从位于高压下的天然气中分离C2+烃馏分的方法，其中精馏所要求的温度和压力值通过热交换和两级有效降压取得，而精馏在两个降压步骤之间进行。
上述一种方法已由德国公开说明书（DE-OS）284933所公开。在这种方法中，据认为最重要的是，精馏的塔顶冷却是通过精馏塔顶产品的有效降压来实现的。
而通过待分裂天然气的有效降压仅可得到中等程度的冷却效果。在自一定量的CO2存在和足够的高压下进行精馏，可避免二氧化碳的凝结。但这种方法再不用外冷时，却要对天然气加较高的压力。
本发明的任务在于，寻找一种上述类型的改善制冷的方法，以使在不加入外冷时仅对待分解的天然气稍稍加压即可实现C2+的分离。
该任务由下列方案解决，即精馏的塔顶冷却主要通过部分冷却后的待分解天然气的有效降压来实现，首先由待冷却的天然气将精馏塔顶产品加热到大约待分解天然气的入口温度左右，然后送入第二降压段，并重新由待冷却天然气加热到大约待分解天然气的入口温度上下。
与德国公开说明书（DE-OS）2849344中的已知方法相反，本发明的塔顶冷却由分解天然气的有效降压来取得，而预冷则由精馏塔顶产品的有效降压来实现。其中本发明的一个基本特征是，将温度约为待分解天然气入口温度的塔顶产品送入一个膨胀机，因为在这种相对较高的温度下可以取得很高的冷却功效。这里的待分解天然气的入口温度是在第一热交换阶段之前的已压缩、干燥并/    或已脱硫的天然气的温度。该温度一般为环境温度，例如在285和320°K（绝对温度）之间。精馏的塔顶产物在降压之前基本上被加热到待分解天然气的入口温度，其中两种流体之间的温差一般为10度（K）以下，大多数在7度（K）之内。
加热的塔顶产物的降压是如此有利地进行，使同时产生50至90度、最好是65至80度的气体冷却，因此可以达到220至240°K的温度。但在个别情况下可以达到的冷却程度主要依赖于可供利用的压差，即基本上依赖于精馏压力和塔顶馏份将要维持的输出压力之间的差值。精馏一般在10至22巴一较好地是在15至18巴的压力下进行选择较高的压力，例如在20至25巴之间，虽然在输出压力保持不变的情况下提高了可用压差，并由此提高了所得冷却功效，但同时却恶化了由待冷却却原料气进行塔体加热（中间加热）的可能性，因而这样一种方案在许多情况下作为整体来看证明是不利的。另一方面，在许多情况下，特别是在含有二氧化碳天然气的分解情况下，为了有把握地避免相对高的沸点组份如二氧化碳的凝结，必须维持一个相对较高的压力，例如15至20巴。
通常在预冷之后的有效降压之前对待分解的天然气要进行冷凝液分离，其中富含重组份的冷凝在节流降压后被直接送入精馏塔中，只有残留的气相被送去进行有效降压。尤其有利的是，待分解天然气的预冷和冷凝液分离分两步进行。其中第一次冷凝液分离在利用有效降压的精馏塔顶产物的间接换热时对天然气实行冷却之后进行，而在利用要加热的塔顶产物的间接换热时对天然气继续冷却的过程中又有其它的组份冷凝出来，这些冷凝液在末冷凝部分的有效降压之前就被分离。
在本发明方法的较好的另一方案中，首先在待分解天然气有效降压之前使分离出的冷凝液过冷，然后送入精馏塔中进行减压。通过用要加热的过程流体的间接换热使冷凝液过冷到精馏塔的顶部温度，一方面能够制取一部分顶冷却，另一方面，这种方案有可能使该冷凝液在有效降压的天然气的上部进入精馏塔，这样可由在顶部加入的冷凝液对降压气体馏份形成一种洗涤作用，从而导致效率增高。此外，这种方案还允许在可能不使冷凝馏份过冷时使天然气的有效降压在稍高一点的温度下进行。由此产生的更高一些的膨胀机运行温度又进一步改善了制冷效果。
本发明方法的其它细节用下面两个在图中所表示的实施例来说明：
图1表示本发明方法的第一实施例;
图2表示本发明方法的另外一个实施例。
在图1所表示的实施例中，将预先净化过并压缩过的天然气经由管路1在环境温度下引入，并在热交换器2冷却到约230°K，此后经由管道3送往第一分离器4以分离在热交换时所形成的冷凝液。基本上为高沸点天然气组份的已冷凝部分由管道5抽出，在阀门6减压到精馏塔内压力，并在精馏塔7的中部引入。未冷凝的天然气组份从分离器4经管路8排出，在换热器9再冷却至约210°K，紧接着由管路10进入一个第二分离器11。在第二次热交换中冷凝的组份经过管道12和节流阀13到达精馏塔7的上部。这股冷凝液和由管5所抽出的冷凝液送往精馏塔7中的输入位置通常都相应于精馏塔7内的温度和平衡状况而确定。未冷凝的天然气部分经由管道14从分离器11排出并在一个汽轮机15中有效地降至精馏塔的压力。降压时天然气冷却，例如到170°K的温度，由此可以提供精馏塔的压力。降压时天然气冷却，例如到170°K的温度，由此可以提供精馏塔的塔顶冷却，已降压的馏份经由管道16送到精馏塔7的顶部。
精馏时落于塔釜的馏份一也即C2+烃馏份一由管道17排出，并在必要时用一台泵18在该过程产品输出之前将它加到更高的输出压。在精馏塔7的顶部得到一种基本不含C2+烃的馏份，该馏份经过管道19抽出并送至换热器9和2，由待冷却的天然气加热至天然气的入口温度。该已热气体经由管道20进入一个第二膨胀汽轮机21，在此由精馏压力大体上降至一个较低的输出压力。在降压时，例如从17巴降至4.5巴，该气体冷却至约230°K，并在它经过管道23送往用户之前，还要经由管道22再次流过换热器2，以便对天然气基本上进行预冷。
为了一方面支持天然气在换热器2中的预冷，另一方面加热精馏塔7的下部，拟定将由第一块塔板的回流经过管道24排出，在换热器2中加热后经过管道25再送回塔釜，并以相应的方式与由管道26从精馏塔7下部引出的馏份再进行热交换，R然后该馏份由管路27送回精馏塔。最后还可以考虑对精馏塔7再有一次中间加热，为此从塔上部经由管道28引入液流，在换热器9中加热后经管道29送回塔内。在换热器9中由该流体取得的制冷量同样转送给待冷却的天然气。
图2所示的实施例与上述实施例的区别仅仅在于，在第二分离器11中形成的冷凝液并不直接在降压后送入精馏塔7，而是先在换热器9中使之过冷。在节流降压13到精馏塔7的压力后冷凝液被送入精馏塔的顶部，其入口位置高于在汽轮机15中降压并由管道16输入的气体的入口位置。将过冷的冷凝液从精馏塔顶部加入，其结果起了从向塔顶上升的蒸汽中附加地洗出C2+烃的作用，因而使得总效率。另一方面，如果保持精馏产量不变，则该方法可为汽轮机15提供有利的运行条件，因为这样可使汽轮机在较高的温度下运行条件，因为这样可使汽轮机在较高的温度下运行，这又可使得汽轮机效率增高，或使所需增加的压力降低。
在按照图2方法的一个具体的实施例中，含有78.35%（所给百分数均为克分子百分数）甲烷、7.3%乙烷、7.9%丙烷、3.6%丁烷、1.8%、C5+烃、0.9%氮和0.18%二氧化碳的净化天然气在压缩到51.4巴后在311°K的温度下经由管道1送入。在换热器2中冷却到234°K后，即有冷凝液形成，该冷凝液除44.2%的甲烷和各0.2%的氮和二氧化碳外是由从天然气中分离出来的C2+烃组成。甲烷浓度为91%以上的未冷凝度为90%以上的未冷凝部分在换热器9中冷却至214°K。这时形成的冷凝液含有约64%的甲烷，各为0.3%DE3氮和二氧化碳以及剩余的大部分以前没有冷凝的C2+烃。该冷凝液在换热器9中过冷，降压到17巴的精馏压力后在172°K的温度下送入精馏塔7的顶部。
在分离器11中形成的仅含5.3%的C2+组份的气态馏份在汽轮机15中有效地降压到17巴的压力，这时在汽轮机出口的温度为17.4°K。
在精馏塔的7塔釜中在299°时形成一种C2+馏份，该馏份仅含0.7%甲烷和0.4%二氧化碳的不纯物质。该方法的C2+收率为96.5%。
在精馏塔7顶部取出的馏份含有97.3%的甲烷，此外为仅仅1.3%的乙烷、0.1%的丙烷、0.1%的二氧化碳和1.2%的氮。
该气体在换热器9和2中加热到304°K后在16.6巴的压力下送入汽轮机21并降压至4.3巴，同时温度降到234°K。在换热器2中重新加热后在304°K和4巴的压力下将该气体送出。
该方法所用汽机15和21的功率分别为208千瓦和472千瓦。这部分分能量可用于例如天然气分解前的压缩。
为了强调与西德公开说明书（DE-OS）2849344中已知方法相比具有显著的优点而进行了比较计算，这些计算基于使用与前述实施相同组成和数量的气体。其中可见，为了满足过程所需的制冷量将由管道1送入的原料气料气流压缩到61巴（以代替本发明方法中的51.4巴），这1导致了能量额外耗费。此外，汽轮机功率也比本发明方法低得多，因为在原料气体和精馏塔顶产品降压时产生的汽轮机功率为312和216千瓦，也即总共为528千瓦，而在本发明方法中总的汽轮机功率为680千瓦。此外仅补充提及，在本发明方法中需要的设备较少（不用三个而只要各两个换热器和分离器）。

Claims (8)

1、借助于精馏从高压下的天然气中分离C2+烃馏份的方法，其中精馏所要求的温度和压力值通过热交换和两级有效降压取得，并且精馏在两个降压步骤之间进行，其特征在于，精馏的塔顶冷却主要通过部分冷却后的待分解天然气的有效降压制得，并首先用待冷却的天然气将精馏的塔顶产物加热到待分解天然气的入口温度左右，然后送到第二降压段，再用待冷却的天然气加热到待分解天然气的入口温度上下。
2、按照权利要求1的方法，其特征是，精馏的塔顶产物在260和310°K之间-较好的是在270和305°K之间-的温度下送入第二降压段而气体在降压时冷却50至90度。
3、按照权利要求1或2的方法，其特征是，精馏在10至22巴-较好的是在15至18巴-的压力下进行。
4、按照权利要求1至3中之一的方法，其特征是，在有效降压前对部分冷却的待分解的天然气进行冷凝液分离并将分离出来的冷凝液降压后送入精馏塔。
5、按照权利要求4的方法，其特征是，具有两次冷凝液分离。
6、按照权利要求5的方法，其特征是，第一次冷凝液分离在换热器中用有效降压的精馏塔顶产物对天然气冷却后进行。
7、按照权利要求4至6中一项的方法，其特征是，对在未冷凝天然气部分的有效降压之前分离出的冷凝液在其进入精馏塔之前进行过冷。
8、按照权利要求7的方法，其特征是，过冷的精馏冷凝液在塔顶高于有效降压的天然气入口送入。
CN85108285.8A 1984-11-12 1985-11-11 从天然气中分离c2+烃馏份的方法 Expired CN1003376B (zh)

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Families Citing this family (37)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB8703751D0 (en) * 1987-02-18 1987-03-25 Costain Petrocarbon Separation of hydrocarbon mixtures
DE3814294A1 (de) * 1988-04-28 1989-11-09 Linde Ag Verfahren zur abtrennung von kohlenwasserstoffen
US4921514A (en) * 1989-05-15 1990-05-01 Air Products And Chemicals, Inc. Mixed refrigerant/expander process for the recovery of C3+ hydrocarbons
US5026408A (en) * 1990-06-01 1991-06-25 Union Carbide Industrial Gases Technology Corporation Methane recovery process for the separation of nitrogen and methane
FR2664263B1 (fr) * 1990-07-04 1992-09-18 Air Liquide Procede et installation de production simultanee de methane et monoxyde de carbone.
US5275005A (en) * 1992-12-01 1994-01-04 Elcor Corporation Gas processing
DE4334256C2 (de) * 1993-10-07 2002-10-31 Linde Ag Verfahren zum Gewinnen einer C¶2¶H¶4¶-reichen Produktfraktion aus einer kohlenwasserstoffhaltigen Einsatzfraktion
US5390499A (en) * 1993-10-27 1995-02-21 Liquid Carbonic Corporation Process to increase natural gas methane content
US5588308A (en) * 1995-08-21 1996-12-31 Air Products And Chemicals, Inc. Recompression cycle for recovery of natural gas liquids
AR007346A1 (es) * 1996-06-05 1999-10-27 Shell Int Research Un metodo para separar dioxido de carbono, etano y componentes mas pesados de una corriente de gas natural a alta presion
NZ549467A (en) * 2004-07-01 2010-09-30 Ortloff Engineers Ltd Liquefied natural gas processing
MX2008013462A (es) * 2006-06-02 2008-10-29 Ortloff Engineers Ltd Procesamiento de gas natural licuado.
US9869510B2 (en) * 2007-05-17 2018-01-16 Ortloff Engineers, Ltd. Liquefied natural gas processing
US9243842B2 (en) * 2008-02-15 2016-01-26 Black & Veatch Corporation Combined synthesis gas separation and LNG production method and system
US20090282865A1 (en) 2008-05-16 2009-11-19 Ortloff Engineers, Ltd. Liquefied Natural Gas and Hydrocarbon Gas Processing
US20100287982A1 (en) * 2009-05-15 2010-11-18 Ortloff Engineers, Ltd. Liquefied Natural Gas and Hydrocarbon Gas Processing
US8434325B2 (en) 2009-05-15 2013-05-07 Ortloff Engineers, Ltd. Liquefied natural gas and hydrocarbon gas processing
CN101967077B (zh) * 2009-07-27 2013-10-16 中国石油天然气股份有限公司 乙烯装置前脱乙烷分离工艺方法
US10113127B2 (en) 2010-04-16 2018-10-30 Black & Veatch Holding Company Process for separating nitrogen from a natural gas stream with nitrogen stripping in the production of liquefied natural gas
US9777960B2 (en) 2010-12-01 2017-10-03 Black & Veatch Holding Company NGL recovery from natural gas using a mixed refrigerant
US10451344B2 (en) 2010-12-23 2019-10-22 Fluor Technologies Corporation Ethane recovery and ethane rejection methods and configurations
US10139157B2 (en) 2012-02-22 2018-11-27 Black & Veatch Holding Company NGL recovery from natural gas using a mixed refrigerant
DE102013013883A1 (de) * 2013-08-20 2015-02-26 Linde Aktiengesellschaft Kombinierte Abtrennung von Schwer- und Leichtsiedern aus Erdgas
US10563913B2 (en) 2013-11-15 2020-02-18 Black & Veatch Holding Company Systems and methods for hydrocarbon refrigeration with a mixed refrigerant cycle
US9574822B2 (en) 2014-03-17 2017-02-21 Black & Veatch Corporation Liquefied natural gas facility employing an optimized mixed refrigerant system
AR100494A1 (es) * 2014-04-22 2016-10-12 Shell Int Research Un proceso para recuperar metano a partir de una corriente gaseosa que incluye metano y etileno
CN104211564B (zh) * 2014-09-16 2016-08-17 天津大学 从氯醇法环氧丙烷废液中提取1,2-二氯丙烷的工业装置和连续精馏方法
US10006701B2 (en) 2016-01-05 2018-06-26 Fluor Technologies Corporation Ethane recovery or ethane rejection operation
US10330382B2 (en) 2016-05-18 2019-06-25 Fluor Technologies Corporation Systems and methods for LNG production with propane and ethane recovery
US20170370641A1 (en) * 2016-06-23 2017-12-28 Fluor Technologies Corporation Systems and methods for removal of nitrogen from lng
US10551118B2 (en) 2016-08-26 2020-02-04 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US10533794B2 (en) 2016-08-26 2020-01-14 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US10551119B2 (en) 2016-08-26 2020-02-04 Ortloff Engineers, Ltd. Hydrocarbon gas processing
US11725879B2 (en) 2016-09-09 2023-08-15 Fluor Technologies Corporation Methods and configuration for retrofitting NGL plant for high ethane recovery
US11543180B2 (en) 2017-06-01 2023-01-03 Uop Llc Hydrocarbon gas processing
US11428465B2 (en) 2017-06-01 2022-08-30 Uop Llc Hydrocarbon gas processing
CA3077409A1 (en) 2017-10-20 2019-04-25 Fluor Technologies Corporation Phase implementation of natural gas liquid recovery plants

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2557171A (en) * 1946-11-12 1951-06-19 Pritchard & Co J F Method of treating natural gas
US2823523A (en) * 1956-03-26 1958-02-18 Inst Gas Technology Separation of nitrogen from methane
DE1501722A1 (de) * 1966-01-13 1969-06-26 Linde Ag Verfahren zur Tieftemperatur-Luftzerlegung zur Erzeugung von hochverdichtetem gasfoermigem und/oder fluessigem Sauerstoff
US3375673A (en) * 1966-06-22 1968-04-02 Hydrocarbon Research Inc Air separation process employing work expansion of high and low pressure nitrogen
US3559417A (en) * 1967-10-12 1971-02-02 Mc Donnell Douglas Corp Separation of low boiling hydrocarbons and nitrogen by fractionation with product stream heat exchange
GB1475475A (en) * 1974-10-22 1977-06-01 Ortloff Corp Process for removing condensable fractions from hydrocarbon- containing gases
US4203741A (en) * 1978-06-14 1980-05-20 Phillips Petroleum Company Separate feed entry to separator-contactor in gas separation
DE2849344A1 (de) * 1978-11-14 1980-05-29 Linde Ag Verfahren zur abtrennung einer c tief 2+ -kohlenwasserstoff-fraktion aus erdgas

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