CN86105431A - 氨或甲醇的生产方法及其所应用的气化器 - Google Patents
氨或甲醇的生产方法及其所应用的气化器 Download PDFInfo
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 57
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 22
- 238000004519 manufacturing process Methods 0.000 title abstract description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 68
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 13
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 12
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 12
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Abstract
本文涉及氨或甲醇生产的方法及其所用的气化器。气化器用以生产合成气，合成气在闭合回路中连续不断地通过反应器和冷却器。氨或甲醇在冷却器中得到，并伴有富甲烷尾气。部分尾气从闭合回路中排除并返回到气化器，在气化器中甲烷经转化反应而产生热，从而提高了此方法的效率。
Description
本发明是关于氨或甲醇的生产方法以及此方法所应用的气化器;特别是在气化器中产生合成气，并经由反应器连续不断循环，而生产氨或甲醇的方法及气化器。
尽管由煤的直接燃烧得到热或产生电能，是煤的热能利用的最传统的方法。然而现又提出了另一些新技术，即将煤转化成更理想的能源形式，如燃料气或液体碳氢化合物，和/或转化成有更高经济价值的化学制品。当煤以某种方式转化成燃料气或化学制品时，为改善其原来的氢碳化，就要从煤中脱碳，或者向煤中加氢。通用的脱碳技术是气化法。
当煤完全气化时，气体产物的主要组分是氢气、一氧化碳、不定数量的甲烷和轻碳氢化合物，此外还有二氧化碳。气体中的二氧化碳可用一般的气体洗涤技术予以去除，即从体系中脱碳。水蒸汽与煤的反应可产生氢气，使氢超过原来煤中的含量，反应的最终产物是氢气和一氧化碳的混合气体，其中氢与一氧化碳的比值可任意调整。这种气体产物常称做“合成气”，它可经反应器或类似装置进一步处理以生产氨或甲醇，这些产物是比较纯的物质，有很多用途。
由合成气生产氨或甲醇的方法，通常是使合成气通过以常规方式操作的反应器。生产氨时是使氮气与氢气化合，生产甲醇时是使一氧化碳与氢气化合。在与反应器组成的闭合回路中通常还包括冷却器或类似装置，气体在此系统中连续不断循环，氨或甲醇在冷却器中基本上冷凝下来并排出以做进一步处理。由冷却器出来的含大量甲烷的尾气再循环至反应器。由于甲烷在此体系中是惰性的，故部分富甲烷的尾气要从回路中连续不断地排除。因为甲烷中含有有用的氢，并且甲烷又是惰性的（代替了所需要的产物），这样就不利于提高氢碳比，所以甲烷产量较高时对方法的效率是有害的。
本发明的目的是提供一种生产氨或甲醇的方法，该方法与现有技术相比有较高的效率。
本发明的再一个目的是提供一种上述类型的方法，该方法利用甲烷的燃烧热，来改进方法的效率。
本发明的进一步的目的是提供一种上述类型的方法，于该方法中使来自反应器的甲烷改道进入气化器作为燃料使用，以代替产生等当量BTU的煤。
本发明的更进一步的目的是提供一种应用于上述方法的气化器。
为达到上述及其他目的，本发明采用流化床气化器，经气化器产生的合成气连续不断地通过闭合回路中的反应器和冷却器。在冷却器中得到氨或甲醇产品以及富甲烷的尾气。部分尾气由闭合回路中排除并返回气化器，在气化器中甲烷经转化反应以产生热，从而提高了方法的效率。
参阅本发明最佳实施例的详细说明及其附图后，就能全面理解上面的概述以及本发明的目的、特点和优点，其中：
图1是本发明的系统原理图。
图2是本发明方法的气化器的立剖面示意图。
最佳实施例
本发明将以生产氨的系统（如图1所示）为例予以说明。图中标号10表示流化床气化器，由管路12供给颗粒状煤，由管路14送入空气。顶部管路16用以排出气化器中产生的合成气，排渣管路18由气化器底部伸出，用以排出乏煤，最好是以结渣形式排出。下面将对气化器作更详细的描述。
合成气在气化器10中生成，主要含有氢气、氮气和甲烷以及一氧化碳、二氧化碳、水蒸汽和硫化氢等。合成气输送至预处理站19，在预处理站使合成气中的一氧化碳和水蒸汽转化为二氧化碳和氢气，同时从合成气中去除二氧化碳和硫化氢，需要时完成最后除硫。因为这些处理均属常规技术，故不再细述。预处理站19的出口经管路20与加工设备相连接，加工设备总体用标号21表示，并用虚线所包围。加工设备21的任务是进一步加工由气化器10来的合成气，并以常规方法生产氨。
加工设备21包括反应器22，反应器22有入口管路23，以导入由气化器10来的合成气。反应器22以常规方式操作，器内装有催化剂，以催化氢气与氮气的化合，由反应器22出来的气体经管路24送至冷却器25。
冷却器25以常规方式操作，冷却由反应器22来的气体，并达到形成液氨的程度。冷却器可利用自动致冷作用以达冷凝要求。液氨经管路26排至外附设备（未画出）以做它用。
冷却器25中的剩余气体，经管路28、清除装置30和管路32，重返入口管路23，以重新进入反应器22。清除装置30以常规方式操作，排放或清除由管路28来的一小部分（例如5%）气体，因为该气体中的甲烷含量较高，而甲烷在前述方法中又是惰性的。用气化器10来的合成气在加工设备21中连续不断循环以制备产品气（于本实施例中是氨）和清除甲烷的这种技术是常规技术，故对此不作进一步细述。
根据本发明的要点，经清除装置30排放的富甲烷气体由管路34输送至气化器10的排渣管道18的内部，对此将在下面描述。
如图2所示，排渣管道18的上端与气化器10的壳体内的倒向截头圆锥形多孔空气分布板40的锥顶部相连，管道18的下端从气化器10的壳体的底部向外伸出。颗粒状煤由管道12送入，煤床42由多孔板40支撑，煤渣和乏煤由管道18排出并送至外附设备（未画出）。
外加的空气和水蒸汽由管道44进入。管道44包括水平部分和垂直部分，水平部分贯穿管道18壁上的合适开孔，垂直部分与管道18同轴向上延伸。管道44的外径要小于管道18的内径，以形成环形通道，使煤渣和乏煤能从煤床42卸出。
管道34包括水平部分和垂直部分，水平部分是从加工设备21延伸而来，并贯穿管道18和管道44管壁上的合适开孔伸进到管道44内，垂直部分在管道44内与管道44同轴向上延伸。管道34的外径要小于管道44的内径，以形成通道使空气和水蒸汽能经管道44进入煤床。
管道34和44的上端都穿过空气分布板的锥顶开孔，向煤床42的底部伸进少许。这样，来自加工设备21的富甲烷气体，便与空气及水蒸汽一起分别经管道34与44进入煤床42。
空气管道14贯穿气化器10的壳体侧壁，较高压力的外加空气经此管道送入气化器。压缩空气向上穿过空气分布板40上的小孔进入煤床42，使颗粒状煤呈流态化并促进其燃烧。
操作时，可调量的压缩空气，经管道14向上穿过多孔板40进入煤床42。同时可调量的压缩空气和水蒸汽，也经管道44导入。需控制所引进空气的流速，使床42上的颗粒状煤呈流态化以促进其燃烧。空气量要控制在不足以使煤完全燃烧，然而却足以产生含氢气、一氧化碳、二氧化碳和少量甲烷的合成气。当然，气化器还装有煤床点火喷咀或类似装置（未画出），以便煤床开工点火。补加煤是通过管道12进入煤床。
气化器10中产生的合成气，与水蒸汽或水一起输送至预处理站19进行上述的预处理，以得到氢气、氮气和甲烷。然后，此气体经管道23进入反应器22。反应器的温度和其他临界条件要按预定方法控制，以使氢气和氮气发生化合反应。产品气与剩余气一起由反应器22排出，通过管道24输送至冷却器25。
冷却器25的作用是按上述方式得到液氨，并经管路26排至外附设备（未画出）。剩余尾气由冷却器25经管路28进入清除装置30。清除装置30的作用是将小部分气体排放或清除至管路34，其余气体由清除装置30经管路32返回至入口管路23，以再循环至反应器22。这样，便由反应器22、冷却器25和清除装置30，组成了一个连续的闭合回路。
从管路34来的富甲烷气体，穿过排渣管道18以与其同轴方向进入流化床42，床中空气里的氧将甲烷转化为一氧化碳和氢气，并与气化器中生成的合成气相混合经管道16排出。由于甲烷的转化产生燃烧热，因而就减少了气化器10中煤的需要量。
由此可以看到，与现有技术相比，由于本发明利用了甲烷的燃烧热，所以其方法和设备具有更高的效率。
显然，此方法也适用于甲醇或任何一种可用上法制得并伴生富甲烷尾气的化学制品的生产。因此，加工设备21也可看成是生产甲醇的整套设备，甲醇的生成反应在反应器22中进行，而在冷却器25得到富甲烷的尾气。按照本发明，尾气被分流，一部分返回到反应器进一步转化为甲醇，另一部分返回到气化器10，第三部分可能经排气口（未画出）排出或另作其他处置。
Claims (11)
1、生产氨或甲醇的方法，包括下述各步骤：颗粒状煤流态化床的形成；氧化剂气体以足够数量和速度穿过煤床，使颗粒状煤呈流态化。并促进其燃烧；控制煤床温度和空气或氧气进入量，使煤气化以产生合成气；以某种方式加工合成气，使其产生氨或甲醇和富甲烷尾气；排除部分尾气并将其送至流化床，使尾气中的甲烷与空气反应发生转化，这就代替了煤床中部分做燃料用的煤。
2、按照权利要求1的方法，还包括向气化器供给水蒸汽的步骤。
3、按照权利要求1的方法，其中所产生的合成气含有氢气、一氧化碳、氮气和水蒸汽;此方法还包括将一氧化碳和水蒸汽转换为二氧化碳和氢气以及从合成气中除二氧化碳的步骤。
4、按照权利要求3的方法，其中甲烷要转化为一氧化碳和氢气，并与合成气中的一氧化碳和氢气相混合。
5、按照权利要求3的方法，其中加工步骤包括氢气与氮气化合产生氨的步骤。
6、按照权利要求4的方法，其中加工步骤还包括合成气的循环步骤，即经反应器完成化合反应以及经冷却器得到氨或甲醇和尾气的循环步骤。
7、按照权利要求6的方法，其中加工步骤还包括剩余尾气经由反应器和冷却器的连续循环步骤。
8、流化床气化器，包括壳体，装于壳体内支撑颗粒状燃料流化床的多孔板;氧化剂气体导入燃料层的装置，它使床层流态化并促其燃烧;甲烷导入燃料层的装置，使甲烷与氧作用转化甲烷从而产生热。
9、按照权利要求8的气化器，其中还包括与多孔板的开孔相连的排渣管道，以从床中排除乏燃料;导入甲烷的装置，它包括一根穿过排渣管道并有部分延伸至燃料层中的输送管。
10、按照权利要求9的气化器，其中空气导入装置包括一根穿过排渣管道并有部分延伸至燃料层中的输送管。
11、按照权利要求10的气化器，其中空气导入装置还包括从多孔板下面向壳体内送气的管道，使空气通过孔眼而进入多孔板。
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US77014085A | 1985-08-28 | 1985-08-28 | |
| US770140 | 1985-08-28 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN86105431A true CN86105431A (zh) | 1987-03-18 |
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ID=25087607
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN198686105431A Pending CN86105431A (zh) | 1985-08-28 | 1986-08-27 | 氨或甲醇的生产方法及其所应用的气化器 |
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| Country | Link |
|---|---|
| EP (1) | EP0217491A1 (zh) |
| JP (1) | JPS6252101A (zh) |
| CN (1) | CN86105431A (zh) |
| AU (1) | AU6039786A (zh) |
| ES (1) | ES2001259A6 (zh) |
| ZA (1) | ZA864784B (zh) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103209946A (zh) * | 2010-11-19 | 2013-07-17 | 三井化学株式会社 | 甲醇的制造方法 |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR843515A (fr) * | 1937-09-27 | 1939-07-05 | Metallgesellschaft Ag | Procédé pour produire du gaz de synthèse par gazéification de combustibles sous pression élevée |
| US2713590A (en) * | 1948-10-28 | 1955-07-19 | Kellogg M W Co | Heat treatment of solid carboncontaining materials |
| US4315758A (en) * | 1979-10-15 | 1982-02-16 | Institute Of Gas Technology | Process for the production of fuel gas from coal |
| US4348487A (en) * | 1981-11-02 | 1982-09-07 | Exxon Research And Engineering Co. | Production of methanol via catalytic coal gasification |
| ZA842807B (en) * | 1983-05-31 | 1984-11-28 | Westinghouse Electric Corp | Gasification process for ammonia production |
| US4524056A (en) * | 1983-07-05 | 1985-06-18 | Foster Wheeler Energy Corporation | Process for the production of ammonia |
-
1986
- 1986-06-27 ZA ZA864784A patent/ZA864784B/xx unknown
- 1986-07-02 EP EP86305138A patent/EP0217491A1/en not_active Withdrawn
- 1986-07-08 JP JP61158887A patent/JPS6252101A/ja active Pending
- 1986-07-21 AU AU60397/86A patent/AU6039786A/en not_active Abandoned
- 1986-08-22 ES ES8601296A patent/ES2001259A6/es not_active Expired
- 1986-08-27 CN CN198686105431A patent/CN86105431A/zh active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103209946A (zh) * | 2010-11-19 | 2013-07-17 | 三井化学株式会社 | 甲醇的制造方法 |
| CN103209946B (zh) * | 2010-11-19 | 2016-06-15 | 三井化学株式会社 | 甲醇的制造方法 |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0217491A1 (en) | 1987-04-08 |
| ES2001259A6 (es) | 1988-05-01 |
| AU6039786A (en) | 1987-03-05 |
| ZA864784B (en) | 1987-02-25 |
| JPS6252101A (ja) | 1987-03-06 |
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