CN107364831B - 通过烃类原料气的催化蒸汽重整产生合成气的方法和设施 - Google Patents
通过烃类原料气的催化蒸汽重整产生合成气的方法和设施 Download PDFInfo
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Abstract
一种用于通过烃类原料气的催化蒸汽重整产生合成气的方法和设施，合成气主要由氢和一氧化碳组成，其中通过产生烟道气来生成发生化学重整反应所需的燃烧器的热，其中通过利用合成气和烟道气中所含的热，从锅炉给水生成纯蒸汽并且从过程冷凝物生成过程蒸汽，其中合成气和烟道气用于生成纯蒸汽，并且纯蒸汽的一部分作为热传递介质用于生成过程蒸汽，纯蒸汽的剩余部分作为输出蒸汽从过程排出。
Description
技术领域
本发明涉及一种用于通过烃类原料气的催化蒸汽重整产生主要由氢和一氧化碳组成的合成气的方法，其中通过产生烟道气来生成发生化学重整反应所需的燃烧器的热，其中通过利用合成气和烟道气中所含的热，从锅炉给水生产纯蒸汽并且从过程冷凝物生成过程蒸汽。
本发明还涉及实施该方法的设施。
背景技术
这类方法和设施是已知的。用于烃类原料气的催化蒸汽重整的基础过程例如描述在Ullmann的《工业化学百科全书》(Encyclopedia of Industrial Chemistry)，第六版，第15卷，气体产生，第2章中。原料气，即烃类气体诸如天然气和蒸汽，在升高的压力如20-35bar和高温如800-950℃下穿过填充有催化剂的外部加热反应管。原料气被转化为富含氢和一氧化碳的合成气。这类管式反应器常常被称作SMR，这类方法被称作SMR方法，SMR是蒸汽-甲烷-重整器(Steam-Methane-Reformer)的缩写。变压吸附过程常常被采用用于从合成气分离氢馏分，这被描述在Ullmann所著的同一卷的第5.5.3章。
为了方法的经济性，非常重要的是将消耗用于加热原料气和用于总体上实施吸热重整反应的热能尽最大可能地用于生成蒸汽。与烃类原料气一起使用的蒸汽称为过程蒸汽。过程蒸汽通过在合成气冷却时从合成气形成和沉积的冷凝物再蒸发而获得。然而，合成气和烟道气的热含量超出生成过程蒸汽所需的热量。为很好地利用该超出的热，将该超出的热用于产生所谓的输出蒸汽(export steam)，输出蒸汽主要用于SMR过程外部。为了不从SMR过程导出带有杂质的输出蒸汽，新鲜的锅炉给水用于生成输出蒸汽。输出蒸汽的一部分用于补偿生成过程蒸汽期间的淘析损失。
合成气和烟道气中所含的热用于生成蒸汽在许多情形中通过在这些气体与过程冷凝物和锅炉进水之间实施间接换热来实现。德国专利DE102010044939B3描述了以这种方式实施的过程。
本发明的目的在于提供一种方法和设施，其中，来自合成气和烟道气用于生成蒸汽的热传递以替代的方式解决。
发明内容
该目标通过根据本发明的用于通过烃类原料气的催化蒸汽重整来产生主要由氢和一氧化碳组成的合成气的方法和根据本发明的用于实施该方法的设施来实现。
根据本发明的方法：
一种用于通过烃类原料气的催化蒸汽重整产生主要由氢和一氧化碳组成的合成气的方法，其中通过产生烟道气来生成发生化学重整反应所需的燃烧器的热，并且，其中通过利用合成气和烟道气中所含的热，从锅炉给水生成纯蒸汽并且从过程冷凝物生成过程蒸汽，其特征在于，合成气和烟道气用于生成纯蒸汽，并且纯蒸汽的一部分作为热传递介质用于生成过程蒸汽，纯蒸汽作的剩余部分作为输出蒸汽从过程排出。
该方法的一个较佳方面特征在于，彼此独立地调节纯蒸汽的作为热传递介质用于生成过程蒸汽的部分和纯蒸汽的作为输出蒸汽从过程排出的部分各自的压力。输出蒸汽的压力常常由过程外部的消耗部要求，输出蒸汽的压力达到52bar。然而，这个压力对于作为热传递介质的蒸汽的过程内部使用并不是最佳的。该方面提供将用于内部应用的压力降低至例如39bar。通过压力的这种减小，蒸汽的冷凝焓增加5.8％，这导致生成过程蒸汽所需的纯蒸汽的量减少。此外，用于生成过程蒸汽的部件可以针对这种较低压力设计，由此降低成本。
根据本发明的设施：
一种用于实施本发明的过程的设施，包括：
-至少一个管式炉，该至少一个管式炉用于实施催化蒸汽重整；
-锅炉，该锅炉用于锅炉给水的热脱气；
-蒸汽锅炉，该蒸汽锅炉用于从锅炉给水生成纯蒸汽；
-至少一个换热器，该至少一个换热器每个都用于通过合成气和烟道气加热和蒸发锅炉给水；
-至少一个装置，该至少一个装置用于将冷凝物与合成气机械分离；
-蒸汽锅炉，该蒸汽锅炉用于生成过程蒸汽，该蒸汽锅炉装配有适于将纯蒸汽用作热传递介质的换热器。
根据本发明的设施的一个优选方面特征在于，存在单独的控制设备来调节和调整纯蒸汽的作为热传递介质用于生成过程蒸汽的部分和纯蒸汽的作为输出蒸汽从过程排出的部分的压力。通过这种装配，蒸汽压力可以单独调节以满足输出蒸汽消耗部的要求和内部过程蒸汽生成的要求。
根据本发明的设施的另一个优选方面特征在于，用于生成过程蒸汽的蒸汽锅炉装配有内板换热器。相对于换热器的外部尺寸，板式换热器提供如此多的换热表面，因此可以将换热器整合到蒸汽锅炉中并由此省略外部换热器。由于这种构造，过程蒸汽生成的设施段所需的空间减少。
根据本发明的设施的另一个较佳方面特征在于，与过程冷凝物和过程蒸汽相接触的设施段由不锈钢制成。由于这种构造，使得能够将杂质诸如CO和CO2留在过程冷凝物中，即过程冷凝物的脱气不会对环境造成负担并且这些组分经由过程蒸汽再次供应到重整过程。由于使用不锈钢，添加用于键合氧和用于pH调节的化学物质可以省略。
附图说明
本发明其它特征、优点和可能的应用可以从以下示例性实施例的描述、标记示例以及附图得到。所描述和/或说明的所有特征自身或以任何组合的方式形成本发明的主题，而不受它们在权利要求中所包含的内容或它们的反向引用的限制。
根据本发明的过程将在下面参照附图的图1加以说明，其中：
图1示出根据本发明的设施的示例性实施例的流程图
具体实施方式
图1：
该流程图示出根据本发明的设施1的示例性实施例，在这个实例中，设施1用于从烃类原料气诸如天然气和蒸汽产生氢。仅示出对于理解发明必不可少的设施或过程的部分。
在设计为管式炉的SMR重整器2中，由天然气3和过程蒸汽4组成的原料气被转化成主要由一氧化碳和氢组成的合成气5。通过燃烧器6加热SMR重整器2，图中仅示出一个燃烧器6，燃烧器6以空气7和燃料气8操作，在燃烧器6中产生烟道气9。为利用合成气5和烟道气9中所含的热，它们都被用作热传递介质用于通过换热器10a和10b加热蒸汽锅炉10，并且此外，合成气5还用于通过换热器20加热天然气3，以及通过换热器11a加热脱气锅炉11。在脱气锅炉11中，锅炉给水12被热脱气，排除气21从设施排出。经由导管13，经脱气和加热的锅炉给水进入蒸汽锅炉10中，在蒸汽锅炉10中，该锅炉给水被蒸发成纯蒸汽14。纯蒸汽14的一部分作为输出蒸汽14a从过程或设施排出，另一部分14b作为加热蒸汽用于加热蒸汽锅炉17，蒸汽锅炉17装配有内板换热器17a。换热器17a中获得的冷凝物经由导管22再循环到脱气锅炉11中。
蒸汽14a和14b的压力每个可以通过阀门23a和23b调节。
在换热器10b中与锅炉给水换热之后，烟道气9从过程中排出用于其它处理。
在冷凝水分离器15中，合成气中形成的水冷凝物16被分离并被引入蒸汽锅炉17中。在此水冷凝物16通过换热器17a被蒸发成过程蒸汽4，其中纯蒸汽14的部分蒸汽用作加热蒸汽14a，即热传递介质，并且随后被引入脱气锅炉11中欧。在冷凝物分离之后，合成气5在变压吸附装置18中被处理，其中，氢馏分19与合成气分离并从设施或过程中排出用于其它处理。氢分离后剩余的残留气8作为燃料气8被供应至SMR重整器2的燃烧器6。
工业实用性
本发明提供一种通过烃类原料气的蒸汽重整产生合成气的替代过程和替代设施。用于产生过程蒸汽的***被重新设计，从而实现能量和结构优点。因此本发明是工业可应用的。
附图标记列表
1 根据本发明的设施
2 SMR重整器
3 天然气流
4 过程蒸汽
5 合成气
6 燃烧器
7 用于燃烧的空气
8 残余/燃料气
9 烟道气
10 用于输出蒸汽的蒸汽锅炉，带有换热器10a,10b
11 脱气锅炉，带有换热器11a
12 锅炉给水，新鲜的
13 锅炉给水，脱气后的
14 纯蒸汽
14a 输出蒸汽
14b 加热蒸汽
15 冷凝物分离器
16 冷凝物
17 用于过程蒸汽的蒸汽锅炉，带有换热器17a
18 变压吸附设施
19 氢
20 换热器
21 从锅炉给水排除的气体
22 用于冷凝物再循环的导管
23 用于调整蒸汽压力的a,b阀门
Claims (4)
1.一种用于通过烃类原料气的催化蒸汽重整来产生主要由氢和一氧化碳组成的合成气的方法，
其中通过产生烟道气来生成发生化学重整反应所需的燃烧器的热，并且
其中通过利用在所述合成气和所述烟道气中所含的热，从锅炉给水生成纯蒸汽，并且
从过程冷凝物生成过程蒸汽，
其特征在于，
合成气和烟道气用于生成所述纯蒸汽，
所述纯蒸汽的一部分作为热传递介质用于生成所述过程蒸汽，并且所述纯蒸汽的剩余部分作为输出蒸汽从过程排出，并且
彼此独立地调节作为热传递介质用于生成过程蒸汽的所述纯蒸汽的所述一部分和作为输出蒸汽从过程排出的所述部分的各自的压力。
2.一种用于实施根据权利要求1所述的方法的设施，包括：
-至少一个管式炉，用于实施催化蒸汽重整，
-用于锅炉给水的热脱气的锅炉，
-用于从锅炉给水生成纯蒸汽的蒸汽锅炉，
-至少一个换热器，所述至少一个换热器每个都用于通过合成气并且通过烟道气加热和蒸发所述锅炉给水，
-用于将冷凝物与所述合成气机械分离的至少一个装置，和
-用于生成过程蒸汽的蒸汽锅炉，所述用于生成过程蒸汽的蒸汽锅炉装配有适于将纯蒸汽用作热传递介质的换热器，
其特征在于，存在独立的控制设备，用于调节和调整作为热传递介质用于生成过程蒸汽的所述纯蒸汽的所述一部分的压力和作为输出蒸汽从过程排出的所述部分的压力。
3.根据权利要求2所述的设施，其特征在于，所述用于生成过程蒸汽的蒸汽锅炉装配有内板换热器。
4.根据权利要求2或3所述的设施，其特征在于，与过程冷凝物和过程蒸汽相接触的设施段由不锈钢制成。
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| EP16400012.7A EP3235785B1 (de) | 2016-04-22 | 2016-04-22 | Verfahren und anlage zur erzeugung von synthesegas mittels katalytischer dampfreformierung eines kohlenwasserstoffhaltigen einsatzgases |
| EP16400012.7 | 2016-04-22 |
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| CN201710307263.0A Active CN107364831B (zh) | 2016-04-22 | 2017-04-24 | 通过烃类原料气的催化蒸汽重整产生合成气的方法和设施 |
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| KR20160060846A (ko) | 2014-11-20 | 2016-05-31 | 삼성전자주식회사 | 디스플레이 장치 및 디스플레이 방법 |
| EP3771688B1 (en) * | 2019-08-02 | 2021-10-27 | Air Products and Chemicals, Inc. | Segregated steam system and process in a hydrogen production facility |
| US20230114501A1 (en) | 2020-04-01 | 2023-04-13 | Topsoe A/S | Process and plant for the production of synthesis gas and generation of process condensate |
| AU2022280346A1 (en) | 2021-05-25 | 2023-10-26 | Topsoe A/S | Process and plant for the production of synthesis gas and generation of process condensate |
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| Publication number | Publication date |
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| KR102354065B1 (ko) | 2022-01-24 |
| SG11201809103PA (en) | 2018-11-29 |
| SA518400272B1 (ar) | 2021-11-06 |
| ES2709688T3 (es) | 2019-04-17 |
| EP3235785A1 (de) | 2017-10-25 |
| US12024428B2 (en) | 2024-07-02 |
| WO2017182140A1 (en) | 2017-10-26 |
| MX368256B (es) | 2019-09-26 |
| EP3235785B1 (de) | 2019-01-02 |
| US20190106323A1 (en) | 2019-04-11 |
| US10894714B2 (en) | 2021-01-19 |
| US20210101797A1 (en) | 2021-04-08 |
| CN207891043U (zh) | 2018-09-21 |
| EA038145B1 (ru) | 2021-07-13 |
| CA3021436A1 (en) | 2017-10-26 |
| MX2018012775A (es) | 2019-01-14 |
| CA3021436C (en) | 2023-08-22 |
| DE102016114120A1 (de) | 2017-10-26 |
| PL3235785T3 (pl) | 2019-04-30 |
| KR20180136971A (ko) | 2018-12-26 |
| CN107364831A (zh) | 2017-11-21 |
| EA201892279A1 (ru) | 2019-03-29 |
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