JP2013516506A - 天然ガスを処理するための装置及び方法 - Google Patents
天然ガスを処理するための装置及び方法 Download PDFInfo
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- JP2013516506A JP2013516506A JP2012546502A JP2012546502A JP2013516506A JP 2013516506 A JP2013516506 A JP 2013516506A JP 2012546502 A JP2012546502 A JP 2012546502A JP 2012546502 A JP2012546502 A JP 2012546502A JP 2013516506 A JP2013516506 A JP 2013516506A
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Abstract
Description
(i)天然ガス流の少なくとも一部を水蒸気と混合する工程と、
(ii)前記混合物を130〜300℃の範囲の吸気口温度で貴金属担持改質触媒に断熱的に通し、メタン、水蒸気、二酸化炭素、一酸化炭素、及び水素を含む改質ガス混合物を生成する工程と、
(iii)前記改質ガス混合物を露点以下に冷却して水を凝縮し、前記凝縮物を除去して脱水改質ガス混合物を供給する工程と、
(iv)前記脱水改質ガス混合物を、酸性ガス回収装置に通し、二酸化炭素、及び少なくとも水素及び一酸化炭素の一部を除去し、それによってメタン流を生成する工程とを含む、天然ガス処理方法を提供する。
(i)天然ガス流に水蒸気を添加する手段と、
(ii)水蒸気を添加する前記手段に作動可能に接続され、貴金属担持改質触媒を含有し、前記混合天然ガス流及び水蒸気が前記触媒を通過し、メタン、水蒸気、二酸化炭素、一酸化炭素及び水素を含む改質ガス混合物を生成するように構成された改質器と、
(iii)前記改質ガス混合物を露点よりも低温に冷却するために前記改質器に作動可能に接続された熱交換手段、及び処理工程凝縮物を回収し、脱水改質ガス混合物を提供するために、前記熱交換手段に作動可能に接続された分離装置と、
(iv)二酸化炭素、並びに前記水素及び一酸化炭素の少なくとも一部を除去し、それによりメタン流を生成するための前記分離装置に作動可能に接続された酸性ガス回収装置と、を含む処理装置を提供する。
天然ガス流と水蒸気の混合物の温度は、例えば、予備加熱器及び/又は水蒸気熱を利用して制御でき、改質器の吸気口で、130〜300℃、好ましくは150〜275℃、より好ましくは160〜200℃、例えば200〜220℃の範囲にある。
好ましくは、水素は、改質原料中に少なくとも一時的に、最大5体積%、より好ましくは最大3体積%、最も好ましくは1〜2体積%の濃度で含まれる。これは、天然ガス流、及び/又は炭化水素と水蒸気の混合物に水素を改質器の上流で供給することで達成できる。このように、水素は、天然ガス流に、任意の水素化脱硫又は飽和器の上流で添加でき、所望により、炭化水素と水蒸気の混合物に、改質装置の上流で添加できる。水素は、容器に入った供給源から得ても、又は水から電気分解で生成しても、あるいはニッケル触媒を含む小規模断熱改質器を用いて、分離天然ガス流若しくは分離改質ガス流の水蒸気改質から生成してもよい。この場合には、メタンを含有する精製された炭化水素流又は改質ガス混合物の少量部分を水蒸気と混合し、混合物を火力ヒーターで加熱し、350〜500℃で触媒を含む断熱水蒸気改質装置を通し、改質原料流として十分な水素を含有する改質ガス混合物を生成することができる。あるいは、又は更に、少量の水素を含有する改質ガス混合物の一部を改質器に再循環してもよい。
生成メタン流を、従来の装置を用いてパイプラインで分配するために更に乾燥し、圧縮してもよく、あるいは、家庭用又は工業用燃料を供給するために天然ガス流と混合し、従来法で処理してもよい。
液化装置への供給がメタン富化天然ガス流を含む場合、望ましくは、メタン富化天然ガス流が、メタン富化流(即ち、液化天然ガス)、エタン流、LPG流(プロパン及びブタンを含む)、及び重質流に分離するように液化装置を操作する。
本発明は、高級炭化水素をメタンに転換することにより、パイプラインの仕様を満たすように富化天然ガス組成を調整するために最適なガス流を提供し、特に、天然ガスの液化と組み合わせる場合に、燃焼及び/又は高級炭化水素の貯蔵と輸送の問題を克服し、LNGの生産を増加させる。LPGの貯蔵を廃止又は削減することで、天然ガスの液化及び貯蔵施設の安全性も向上する。その上、比較的高い融点を有する高級炭化水素、特にC5以上の炭化水素を除去すると、酸性ガス除去装置内での凝固及び発泡によって引き起こされる閉塞等の問題が克服される。本発明を図を参照して、更に説明する。
図2は、第1の態様による処理工程を示すフローチャートである。
図4は、富化天然ガス流をLNG流及び1つ以上の高級炭化水素流に変換するように構成された第3の態様による処理工程を示すフローチャートである。
図1において、浮遊式LNG生産装置100に、天然ガスが供給される水銀除去装置102、脱硫装置104、脱硫天然ガスに水蒸気を添加する飽和器106、改質器108、熱交換及び処理工程凝縮物分離装置110、酸性ガス分離装置112、ガス乾燥装置114、及び貯蔵タンク120に貯蔵する液化天然ガス流118を生成する液化装置116が設置されており、それぞれが互いに機能的に連結している。分離装置110から回収した処理工程凝縮物は、ライン122を経て飽和器106に供給され、蒸気の一部を生成する。
更に、所望により、乾燥器568と熱交換器570との間で、精製し、CO2除去して乾燥させたメタン富化天然ガス流を予備分離装置(不図示)(この装置は、天然ガスから高級炭化水素の一部を分離し、高級炭化水素気化装置に供給されるガス状高級炭化水素流を形成する膜を含む)に通してもよい。
1)Marsa El Braga Libya (Wobbe 53.26 MJ/m3)のLNG
メタン:83.68%
エタン:11.73%
プロパン類:3.51%
ブタン類:0.28%
窒素:0.8%
2)ADGAS UAE (Wobbe 53.48 MJ/m3)のLNG
メタン:84.0%
エタン:14.0%
プロパン類:1.0%
ブタン類:0.9%
窒素:0.1%
処理工程を、水蒸気:炭素比(水蒸気の高級炭化水素に対する比)を2:1で操作する場合は、改質器の吸気口温度と改質圧力は望ましくは、以下の通りである。
圧力(絶対絶対バール) 10 70 100
3)天然ガス
メタン:70%
エタン:15.0%
プロパン類:5.0%
ブタン類:5.0%
ペンタン類:2.0%
窒素:3.0%
処理工程を、水蒸気:炭素比(水蒸気の高級炭化水素に対する比)を2:1で操作する場合は、改質器の吸気口温度と改質圧力は望ましくは、以下の通りである。
圧力(絶対絶対バール) 10 70
また、あるいは、液化天然ガスの生産量は、天然ガス液のメタンへの変換によって増加できる。下記の表は、本発明の方法を用いた場合のLNG生産量の増加の見込みを示す。
Claims (35)
- メタン及び1種以上の高級炭化水素を含む天然ガス流の処理方法であって、
(i)該天然ガス流の少なくとも一部を水蒸気と混合する工程と、
(ii)該混合物を130〜300℃の範囲の吸気口温度で貴金属担持改質触媒に断熱的に通し、メタン、水蒸気、二酸化炭素、一酸化炭素、及び水素を含む改質ガス混合物を生成する工程と、
(iii)該改質ガス混合物を露点以下に冷却して水を凝縮し、該凝縮物を除去して脱水改質ガス混合物を供給する工程と、
(iv)該脱水改質ガス混合物を、酸性ガス回収装置に通し、二酸化炭素、並びに該水素及び一酸化炭素の少なくとも一部を除去し、それによってメタン流を生成する工程と、を含む、方法。 - 該天然ガス流が、固定式沖合施設、又は浮遊式LNG生産装置等の浮遊式沖合施設から選択される沖合処理施設にて処理される、請求項1に記載の方法。
- 該天然ガス流中のメタンの量が、25〜99体積%、好ましくは50〜95体積%の範囲にある、請求項1又は2に記載の方法。
- 該天然ガス流が、随伴ガス、シェールガス、タイトサンドガス、若しくは炭層メタンを含む天然ガス、又は、メタン及び1種以上の高級炭化水素を含む合成天然ガス混合物である、請求項1〜3のいずれか一項に記載の方法。
- 該メタン流をLNG液化装置にて液化する工程を更に含み、
ここで、該天然ガス流が1種以上の高級炭化水素を含有する天然ガスであり、該天然ガス液化工程がメタンのみを処理してLNGとし、液化高級炭化水素が生成しないように天然ガス流が該改質段階に供給される、請求項1〜4のいずれか一項に記載の方法。 - 該天然ガス流が天然ガス原料流の一部を含み、残りの部分を該脱水改質ガス混合物流、又はメタン流と混合し、メタン富化天然ガス流を生成する、請求項1〜4のいずれか一項に記載の方法。
- 更に、LNG液化装置にて該メタン富化天然ガス流を液化する工程を含む請求項6に記載の方法。
- 該液化装置において分離された1種以上の高級炭化水素が、該天然ガス流の一部として改質器に供給される、請求項7に記載の方法。
- 該天然ガス流はメタン富化天然ガスの一部及び1種以上の高級炭化水素を含有し、該メタン富化天然ガスが天然ガス原料を該脱水改質ガス混合物と混合し、該混合物を該酸性ガス回収装置に供給し、そこからメタン富化天然ガスを回収することによって生成され、該1種以上の高級炭化水素が、該メタン富化天然ガスの更なる一部を液化及び分留することによって生成される、請求項1〜4のいずれか一項に記載の方法。
- 該天然ガス流と水蒸気との混合よりも上流で水銀を除去するために、該天然ガス流を水銀の除去に適した精製材料を含む精製装置を通すことにより、該天然ガス流を精製することを含む、請求項1〜9のいずれか一項に記載の方法。
- 該天然ガス流と水蒸気との混合よりも上流で硫黄化合物を除去するために、該天然ガス流を硫黄化合物の除去に適した精製材料を含む精製装置を通すことにより、該天然ガス流を精製することを含む、請求項1〜10のいずれか一項に記載の方法。
- 該水蒸気を該天然ガス流と飽和器を用いて混合する、請求項1〜11のいずれか一項に記載の方法。
- 該改質触媒に供給される該天然ガス/水蒸気の混合物の吸気口温度が、150〜275℃の範囲にある、請求項1〜12のいずれか一項に記載の方法。
- 該改質触媒に供給される該天然ガス/水蒸気の混合物の圧力が、10〜100絶対バールの範囲にある、請求項1〜13のいずれか一項に記載の方法。
- 水素が、少なくとも一時的に、該天然ガス/水蒸気の混合物に、最大5体積%、好ましくは最大3体積%の濃度で含まれる、請求項1〜14のいずれか一項に記載の方法。
- 該貴金属担持改質触媒が、Pt、Pd、Ir、Rh又はRuの少なくとも一種を0.1〜10重量%の範囲で含む、請求項1〜15のいずれか一項に記載の方法。
- 該改質工程が、10〜70バールの範囲の圧力で、160〜220℃の範囲の吸気口温度でルテニウム担持触媒を通して操作される、請求項1〜16のいずれか一項に記載の方法。
- 1種以上の熱交換器内で、該改質ガス混合物と水の間で熱交換し、該改質工程で使用する水蒸気の少なくとも一部を生成することを含む、請求項1〜17のいずれか一項に記載の方法。
- 該処理工程凝縮物の少なくとも一部が、該天然ガス流と混合する該水蒸気の少なくとも一部を生成するために使用される、請求項1〜18のいずれか一項に記載の方法。
- 該酸性ガス回収装置が、膜、又は物理洗浄溶媒系、又はアミン洗浄系を含む、請求項1〜19のいずれか一項に記載の方法。
- 該メタン流を、乾燥装置を用いて乾燥することを含む、請求項1〜20のいずれか一項に記載の方法。
- メタン及び1種以上の高級炭化水素を含む天然ガス流の処理装置であって、
(i)天然ガス流に水蒸気を添加する手段と、
(ii)水蒸気を添加する該手段に作動可能に接続され、貴金属担持改質触媒を含み、該混合天然ガス流及び水蒸気が該触媒を通過し、メタン、水蒸気、二酸化炭素、一酸化炭素及び水素を含む改質ガス混合物を生成するように構成された改質器と、
(iii)該改質ガス混合物を露点よりも低温に冷却するために該改質器に作動可能に接続された熱交換手段、及び、処理工程凝縮物を回収し、脱水改質ガス混合物を提供するために、該熱交換手段に作動可能に接続された分離装置と、
(iv)二酸化炭素、並びに該水素及び一酸化炭素の少なくとも一部を除去し、それによりメタン流を生成するための該分離装置に作動可能に接続された酸性ガス回収装置と、を含む処理装置。 - 該メタン流の少なくとも一部を液化するための該酸性ガス回収装置に作動可能に接続した天然ガス液化装置を更に含む、請求項22に記載の装置。
- 固定式沖合施設、又は浮遊式LNG生産装置等の浮遊式沖合施設から選択される沖合天然ガス処理施設の一部を形成する、請求項23に記載の装置。
- 随伴ガス、シェールガス、タイトサンドガス、若しくは炭層メタンを含む天然ガス、又はメタン及び1種以上の高級炭化水素を含む合成天然ガスを、水蒸気を添加する手段に供給する手段を含む、請求項22〜24のいずれか一項に記載の方法。
- 水銀の除去に適した精製材料を含み、水蒸気を添加する該手段の上流に設置された精製装置を含む、請求項22〜25のいずれか一項に記載の装置。
- 硫黄化合物の除去に適した1種以上の精製材料を含み、水蒸気を添加する該手段の上流に設置された脱硫装置を含む、請求項22〜26のいずれか一項に記載の装置。
- 該改質器に供給される該天然ガス流及び所望により該水蒸気の一部を通し、該脱硫器の上流に設置された火力ヒーターを含む、請求項27に記載の装置。
- 水蒸気を添加する該手段が飽和器を含む、請求項22〜28のいずれか一項に記載の装置。
- 該水蒸気改質器が、Pt、Pd、Ir、Rh、又はRuの内の1種以上を0.1〜10重量%含む貴金属担持触媒を含む断熱水蒸気改質器である、請求項22〜29のいずれか一項に記載の装置。
- 該改質ガス混合物と水との間で熱交換し、該改質工程にて使用される該水蒸気の少なくとも一部を生成するように構成された1つ以上の熱交換器を含む、請求項22〜30のいずれか一項に記載の装置。
- 該分離装置が、該回収凝縮物の少なくとも一部が該天然ガス流と混合する該水蒸気の少なくとも一部の生成に使用されるように、該天然ガス流に水蒸気を添加する該手段に作動可能に接続される、請求項22〜31のいずれか一項に記載の装置。
- 該酸性ガス回収装置が、膜、又は物理洗浄溶媒系、又はアミン洗浄系を含む、請求項22〜32のいずれか一項に記載の装置。
- 該メタン流を乾燥する乾燥装置を含む、請求項22〜33のいずれか一項に記載の方法。
- 天然ガスを該脱水改質ガス混合物、又はメタン流と混合し、メタン富化天然ガスを提供するように構成された混合装置を含む、請求項22〜34のいずれか一項に記載の方法。
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EP2521761A1 (en) | 2012-11-14 |
EP2521761B1 (en) | 2015-11-25 |
US10010858B2 (en) | 2018-07-03 |
BR112012016576B1 (pt) | 2018-08-07 |
MY162747A (en) | 2017-07-14 |
DK2521761T3 (en) | 2016-02-29 |
AU2010340809B2 (en) | 2016-01-28 |
US20130090505A1 (en) | 2013-04-11 |
CN102762701A (zh) | 2012-10-31 |
GB201000097D0 (en) | 2010-12-29 |
WO2011083297A1 (en) | 2011-07-14 |
KR20120121894A (ko) | 2012-11-06 |
CN102762701B (zh) | 2015-05-20 |
US9284236B2 (en) | 2016-03-15 |
AU2010340809A1 (en) | 2012-08-02 |
US20160144335A1 (en) | 2016-05-26 |
KR101788346B1 (ko) | 2017-10-19 |
BR112012016576A2 (pt) | 2016-04-12 |
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