CN110217757A - 具有降低的二氧化碳产生和较高的碳和热效率的整合的煤液化、石油或生物质设备 - Google Patents

具有降低的二氧化碳产生和较高的碳和热效率的整合的煤液化、石油或生物质设备 Download PDF

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CN110217757A
CN110217757A CN201910155035.5A CN201910155035A CN110217757A CN 110217757 A CN110217757 A CN 110217757A CN 201910155035 A CN201910155035 A CN 201910155035A CN 110217757 A CN110217757 A CN 110217757A
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carbon
methanol
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J.J.科尔亚
J.E.杜迪
E.D.皮尔
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Axens SA
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Abstract

本发明的主题为在煤液化、石油精制或生物质转化设备内整合生产氢气和甲醇，导致获得较低的二氧化碳（CO2）生产、净排放和较高的碳和热效率的出乎预料的益处。

Description

具有降低的二氧化碳产生和较高的碳和热效率的整合的煤液 化、石油或生物质设备
本发明的主题为在煤液化、石油精制或生物质转化设备内整合生产氢气和甲醇，导致获得较低二氧化碳（CO2）产生和较高碳和热效率的出乎预料的益处。
申请人已经意识到在煤液化、石油精制或生物质转化设备内具有与甲醇装置整合的氢气装置存在很多优势，从而例如提供裂化/改质(upgrading)需要的氢气和生产M15汽油的精制需要的甲醇。
本发明涉及天然气的蒸汽甲烷重整(SMR)和用于甲醇和高纯度氢气二者的生产的粗合成气的明智使用。在精制、煤液化或生物质设备中，在初级和次级改质单元中使用氢气。在这些设备中，甲醇可以用于生产杂合轻质燃料（包括M15汽油）和/或能够作为燃料产品共混物或石油化工原料而输出。
申请人的创新工艺结构导致获得一些相对于现有技术从未预料的优势。首先，在转化设备中的氢气/甲醇装置的整合导致获得产生的CO2的量/单位产生的净液体的降低。此外，这个整合的工艺改善了碳效率（进料碳对液体产品的比率）以及热效率（原料热值对液体产品的比率）。
另外，相对于使用新鲜的和未转化的煤的气化来生产需要的氢气的现有技术水平的煤液化设备，申请人的发明的工艺结构的应用导致获得碳效率、项目净收益和项目内部收益率(IRR)的提高。
独特的工艺结构也是优化的方法，其中最有效地使用了进料煤和天然气原料中的碳，如由产生的CO2的降低和碳和热效率的提高证实地。另外，利用大的粗合成气比率的单程甲醇合成装置的规范导致获得降低的资金和操作成本。最后，申请人的工艺结构通过M15的生产和净甲醇的生产而最大化汽油产品比率，其还有助于改善碳利用、装置热效率、高液体产率和改善的项目收益和收益率。
更具体地，申请人的本文教导一种同时降低二氧化碳（CO2）产生和净二氧化碳排放的整合方法，其同时改善重质烃加工设备的碳和热效率，该方法包括：
（a）使用蒸汽甲烷重整器和单程甲醇生产单元生产高纯度氢气料流和甲醇料流；
（b）将一部分所述氢气料流进料至加工重质烃料流以形成液体料流的加氢裂化单元；
（c）将来自步骤a）的一部分所述甲醇料流和一部分所述氢气料流与来自步骤b）的所述液体料流一起进料至液体改质单元以形成一种或多种可出售汽油料流。
附图的简要说明
图1示出使用煤液化设备作为一个实例来示例申请人的发明的本发明的流程框图。
具体实施方式
图1示例申请人的在煤液化设备中应用的工艺结构。将进料煤10进料至煤预备(preparation)20用于干燥和定型(sizing)，然后进料至直接煤液化综合设施30，其包括一个或多个煤液化反应器。直接煤液化(DCL)为使溶剂（未示出）中的煤10与氢气在高温高压下反应以产生液体燃料的方法。在煤液化综合设施30中，使用固体挤出物催化剂（未示出）和氢气22a将煤转化成粗液体38和气体36产品。上述的用于煤液化单元的氢气料流22a在蒸汽甲烷重整器和甲醇合成综合设施16中形成。
采用蒸汽进行的天然气的重整称为蒸汽甲烷重整(SMR)，并为生产商业的大体积氢气的有效方法。在申请人的发明中，蒸汽甲烷重整器和甲醇合成综合设施16包括蒸汽重整器反应器单元（未示出）、炉段（未示出）和甲醇生产单元。在图1中未示出涉及蒸汽甲烷重整器和甲醇合成综合设施16的详细内容，但可以在下文中进行描述。
蒸汽甲烷重整器反应器单元在高温（700-1100℃）下和在基于金属的催化剂的存在下操作。在蒸汽重整器反应器单元中，蒸汽料流2与天然气4中的烃根据下式反应以产生一氧化碳和氢气：
。
在蒸汽重整器反应器单元中发生的其他反应包括根据下式的水煤气变换：
。
初级SMR反应是高度吸热的并需要高温来获得可接受的甲烷转化率。SMR方法的大能量需要由在蒸汽重整器综合设施的炉段中发生的燃烧反应获得。来自蒸汽重整器反应器单元的产品为合成气体料流，也称为主要含有CO、CO2、H2、H2O和未反应的CH4的合成气（未示出）。
将粗SMR合成气按线路送至甲醇生产单元，其中一氧化碳和二氧化碳使用催化剂反应产生甲醇和水。该反应是放热的并且过量的能量可以用于降低SMR反应器燃料需求。由于在主题发明中消耗相对大量的氢气，与高比率的合成气一致，甲醇合成装置是单程的（即没有再循环）。
将包含与SMR粗气中相同组分的来自甲醇装置的吹扫合成气按线路送至变换单元。在变换单元中，伴随产生另外的二氧化碳，一氧化碳转移向氢气。将来自变换单元的产品气体送至二氧化碳移除单元，其选择性地吸附来自该气体的二氧化碳28。将来自CO2吸附器单元的富含氢气的产品在导致获得氢气产品22的最终的膜或吸附单元中进一步纯化。该氢气22气体包含超过99 V%的氢气并随后可用于初级转化和次级改质单元。之后进一步纯化并压缩二氧化碳料流28并且为最终产品。
将来自SMR/甲醇综合设施16的一部分甲醇26和一部分氢气22b与来自煤液化综合设施30的液体产品38一起按线路送至液体改质单元48从而产生例如包括M15汽油、56、柴油57和减压瓦斯油(VGO)58产品的可出售燃料产品。将在液体改质单元48中未使用的甲醇料流26的部分作为最终产品26b输出。
将来自煤液化综合设施30的粗气体产品36与来自液体改质装置48的粗气产品55一起送至轻质终产品回收单元50以例如生产燃料气52和液化石油气(LPG)54（包括丙烷、丁烷和其混合物）用作精制燃料或用作净产品。将在轻质终产品回收段50中回收的各较重组分（如料流51所示）共混回到液体改质单元48，其主要用于M15汽油生产。
本发明通过下文的实施例情况进一步描述和理解，其不应该被理解为限制本发明的范围。
实施例
直接煤液化研究
研究美国产的直接煤液化设备以示例本发明的优点。商业规模的设备具有8000 MTPD（干基）的含沥青煤以产生可出售液体燃料。开发三个商业实例以评估总体装置产率和包括收益率在内的经济效益。前两个实例（1和2）不具有任何甲醇生产。在全部实例中，煤在高压、高温沸腾床反应器系统中液化并且处理产品从而可出售。在所有实例中输入电能，除了在设备中发电的实例1。捕获、纯化并压缩来自SMR或气化器（只在实例1中使用）的一部分二氧化碳。
在下文中描述三个实例：
实例1—通过来自液化单元的未转化煤和附加的新鲜煤的蒸汽-氧气气化来提供初级转化和加氢处理单元需要的氢气。没有甲醇生产。没有SMR单元。在这个实例中包括空气分离装置以产生用于气化器的氧气。
实例2—通过天然气进料的SMR代替气化器来提供需要的氢气。没有甲醇生产。将直接煤重质残渣（包括未转化的煤和灰分）送至装置的界区(battery limits)以作为燃料出售。
实例3—这个实例与实例2相同，除了将SMR粗气首先按线路送至甲醇生产之外。这是使用申请人的发明的工艺结构。甲醇产品的生产率足以提供M15汽油产品和甲醇输出。
在表2和3中概括商业研究的技术和经济效果。在下表1中示出重要的假定。
表1—重要假定
两个基础实例（1和2）示例用于生产需要的氢气的SMR和气化之间的区别。所捕获的二氧化碳对于气化的实例较高，但碳效率（进料碳对液体产品的比率）显著较低（57 vs.49%）。对于气化的实例，排放至大气中的碳也高得多。气化实例具有较高的投入和显著较低的IRR。相对于基于SMR的氢气生产，较低的收益率通常是明显的，在于天然气价格低于大约$10/MM Btu。
在实例3中的M15汽油的生产和过量甲醇的输出比实例2具有更高水平的碳效率（58.5 vs. 57.0%），表明甲醇的增量产生是天然气的有效使用并将导致每单位的产生的液体的量较低的二氧化碳产生。这示于表2中，其中所排放的二氧化碳以每1000桶液体产品表示，对于实例3相比于实例2，碳排放低8%（92.6 vs. 100.6 ST/1000Bbl）。这是本发明的显著成果。相比于实例2，还存在总体装置热效率的1.4个百分点的提高。
相比于实例2，实例3具有高21%的液体产生。这是由于生产甲醇的6357BPSD和用于生产M15汽油的1968BPSD以及输出的4389 BPSD。如表3中所示，实例3具有显著较大的装置每年净利润（$516 vs. $416MM）和较高的项目收益率。这些经济效果也是重要的研究成果。
表2
技术效果
表3
经济效果
本文中所述的发明已经以具体实施方案和应用的形式公开。然而，这些细节并非意在限制，并且其他实施方案由于这个教导对于本领域技术人员是明显的。因此，理解附图和描述是本发明理念的示例，并且不应该理解为限制其范围。

Claims (7)

1.一种同时降低二氧化碳（CO2）产生和净CO2排放的整合方法，其同时改善重质烃加工设备的碳和热效率，该方法包括：
（a）使用蒸汽甲烷重整器和甲醇生产单元生产高纯度氢气料流和甲醇料流；
（b）将一部分所述氢气料流进料至加工重质烃料流以形成液体料流的加氢裂化单元；
（c）将来自步骤a）的一部分所述甲醇料流和所述氢气料流与来自步骤b）的所述液体料流一起进料至液体改质单元以形成一种或多种可出售的汽油料流。
2.根据权利要求1所述的方法，其中所述烃加工设备为煤液化装置。
3.根据权利要求1所述的方法，其中所述烃加工设备为生物质装置。
4.根据权利要求1所述的方法，其中所述烃加工设备为石油装置。
5.根据权利要求1所述的方法，其中以每1000桶所产生的液体产品表示的所述烃加工设备的碳排放降低至少八个百分点（8%）。
6.根据权利要求1所述的方法，其中以每1000桶所产生的液体产品表示的所述烃加工设备的碳排放降低至少五个百分点（5%）。
7.根据权利要求1所述的方法，其中以进料碳对所产生的液体产品的百分比表示的重质烃加工设备的碳效率提高至少一点五个百分点（1.5%）。
CN201910155035.5A 2018-03-02 2019-03-01 具有降低的二氧化碳产生和较高的碳和热效率的整合的煤液化、石油或生物质设备 Pending CN110217757A (zh)

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