JP2006520739A - 水素製造用の自己熱改質装置−改質交換器の配置 - Google Patents
水素製造用の自己熱改質装置−改質交換器の配置 Download PDFInfo
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Abstract
Description
本発明は自己熱改質装置(ATR)および改質交換器を用いた合成のガス(合成ガス)製造に関する。
本発明は自己熱反応器(ATR)と同時に改質交換器を用い、新規水素プラントにおいては資本費用を削減し、エネルギー必要量を低下させ、操業を容易とさせ、そしてNOxとCO2放出量を低減させ、或いは現存水素プラントにおいては水素プラントからの蒸気搬出を削減して水素生産能力を40〜60パーセント程度増強できる。
本発明によるプロセスの一つの実施形態は図1に示した全体的な配置を有している。ライン2から供給される脱硫天然ガスまたは他の炭化水素はライン4からのプロセス蒸気と混合され、当該混合物は供給原料予熱用熱交換器6中にて予熱される。当該混合物の炭素に対する蒸気の比率は望ましくは2.0から4.0で、例えば約3である。予熱した蒸気−炭化水素混合物の第一の部分はライン8を経由して自己熱改質装置(ATR)10中のバーナーに送り込まれ、第二の部分はライン12を経由して改質交換器14の管側導入口に供給される。望めば、更なる蒸気をライン36経由でライン8に追加することができる。
Claims (23)
- 水素を製造する方法であって:
自己熱反応器中で第一の炭化水素部分を蒸気および空気と共に温度650℃から1050℃において接触改質して第一の合成ガス流出物を製造し;
当該第一の合成ガス流出物を改質交換器に供給し;
第二の炭化水素部分を蒸気とともに当該改質交換器中の触媒ゾーンを通過させて第二の合成ガス流出物を生成し;
当該第二の合成ガス流出物を導入口に隣接する触媒ゾーンから放出して当該第一の合成ガス流出物との合成ガス混合物を形成させ;
当該混合物を間接的熱交換にて当該触媒ゾーンを通過させて、それにより当該混合物を冷却すると共に当該触媒ゾーンを加熱し;
当該改質交換器の流出口から当該冷却した混合物を収集し;
当該混合物を転化して一酸化炭素が少なく二酸化炭素に豊むガス流を得て;そして
二酸化炭素に富むガス流を分離して窒素と二酸化炭素を含み水素に乏しい混合ガス流と水素に富む生成物流を形成させる;
ことを含む、水素を製造する方法。 - 当該混合ガス分離は膜分離を含む、請求項1の方法。
- 当該混合ガス分離は圧力スイング吸着を含む、請求項1の方法。
- 当該触媒ゾーンは触媒管を含み、
当該方法は更に:
当該第一の合成ガス流出物を改質装置の管外側に供給すること;
当該第二の炭化水素部分を蒸気とともに当該触媒管を通して供給すること;
当該第二の合成ガス流出物を当該管外側導入口に隣接する触媒管から放出させて合成ガス混合物を形成させること;
を含む、請求項1の方法。 - 当該自己熱改質装置は過剰な空気により運転される、請求項1の方法。
- 当該転化からの二酸化炭素に富むガス流が、3未満の窒素に対する水素のモル比を含む、請求項1の方法。
- 当該混合ガス分離は極低温分離の必要がない、請求項1の方法。
- 空気分離の必要がない、請求項1の方法。
- 当該最初及び第二の炭化水素部分の合計に対する当該第一の炭化水素部分の比率が55から85パーセントである、請求項1の方法。
- 当該最初及び第二の炭化水素部分の合計に対する当該第一の炭化水素部分の比率が60から8パーセントである、請求項1の方法。
- 当該水素生成物流が少なくとも70容量パーセントの純度を有する、請求項1の方法。
- 当該水素生成物流が90から99.5容量パーセントの純度を有する、請求項1の方法。
- 当該水素生成物流が少なくとも95容量パーセントの純度を有する、請求項1の方法。
- 当該水素生成物流が少なくとも97容量パーセントの純度を有する、請求項1の方法。
- 当該水素生成物流が少なくとも98.5容量パーセントの純度を有する、請求項1の方法。
- 請求項1の方法を含み、当該水素に富む生成物流を燃料電池に供給する、電流を発生させる方法。
- 請求項1の方法を含み、当該水素に富む生成物流を水素化処理装置に供給する、水素化処理方法。
- 合成ガスを調製する装置であって:
650℃から1050℃の温度において第一の合成ガス流出物を製造するのに、蒸気及び空気により第一の炭化水素部分を接触改質するための自己熱反応器手段;
当該第一の合成ガス流出物を改質交換器の導入口に供給する手段;
当該改質交換器中の触媒ゾーン内に第二の炭化水素部分を蒸気とともに通過させて第二の合成ガス流出物を形成させる手段;
当該導入口に隣接する触媒ゾーンから当該第二の合成ガス流出物を放出して当該第一の合成ガス流出物との合成ガス混合物を形成させる手段;
当該混合物につき当該触媒ゾーンを横断して通過させ、間接的熱交換により当該混合物を冷却し、当該触媒ゾーンを加熱させる手段;
当該冷却した混合物を当該改質交換器の排出口より収集する手段;
当該混合物を転化して一酸化炭素が乏しくて二酸化炭素に富むガス流を得る手段;および
当該二酸化炭素に富むガス流を分離して、窒素と二酸化炭素を含み水素に乏しい混合ガス流と水素に富む生成物流を形成させる手段;
を含む、合成ガスを調製する装置。 - 当該分離手段は圧力スイング吸着装置を含む、請求項18の装置。
- 当該分離手段は膜分離器を含む、請求項18の装置。
- 当該改質、転化および混合ガス分離は10から200バールのプロセス圧力を含む、請求項1の方法。
- 当該改質、転化および混合ガス分離は少なくとも30バールのプロセス圧力を含む、請求項1の方法。
- ガスタービン駆動により当該接触改質へ空気を圧縮すること、及び、ガスタービンより出る排気から熱を回収することを更に含む、請求項1の方法。
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US32001503P | 2003-03-18 | 2003-03-18 | |
US60/320,015 | 2003-03-18 | ||
PCT/US2004/007952 WO2004083114A2 (en) | 2003-03-18 | 2004-03-12 | Autothermal reformer-reforming exchanger arrangement for hydrogen production |
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US (2) | US7220505B2 (ja) |
EP (1) | EP1603995B1 (ja) |
JP (1) | JP4745219B2 (ja) |
CN (1) | CN100564495C (ja) |
AU (1) | AU2004221826B2 (ja) |
BR (1) | BRPI0408349A (ja) |
CA (1) | CA2507922C (ja) |
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US20070217989A1 (en) | 2007-09-20 |
EP1603995B1 (en) | 2018-05-30 |
RU2343109C2 (ru) | 2009-01-10 |
CA2507922C (en) | 2012-08-14 |
WO2004083114A3 (en) | 2005-04-21 |
AU2004221826A1 (en) | 2004-09-30 |
NZ540784A (en) | 2007-02-23 |
WO2004083114A2 (en) | 2004-09-30 |
EP1603995A4 (en) | 2008-07-02 |
US7550215B2 (en) | 2009-06-23 |
CA2507922A1 (en) | 2004-09-30 |
CN1860207A (zh) | 2006-11-08 |
RU2005132171A (ru) | 2006-02-10 |
BRPI0408349A (pt) | 2006-03-21 |
AU2004221826B2 (en) | 2009-12-17 |
CN100564495C (zh) | 2009-12-02 |
JP4745219B2 (ja) | 2011-08-10 |
US7220505B2 (en) | 2007-05-22 |
EP1603995A2 (en) | 2005-12-14 |
US20040182002A1 (en) | 2004-09-23 |
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