JP5478505B2 - ディーゼル範囲炭化水素を製造するためのバイオ原料の多段共処理 - Google Patents
ディーゼル範囲炭化水素を製造するためのバイオ原料の多段共処理 Download PDFInfo
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Description
次の実施形態においては、鉱油炭化水素原料材およびバイオ成分原料材は、多段反応系で共処理される。好ましくは、鉱油炭化水素原料材は、T5〜T95範囲300〜775°Fのディーゼル沸点範囲原料材である。原料材のバイオ成分部分は、組み合わせ原料材の約0.1〜約50wt%を占めることができ、約20wt%以下、または約15wt%以下、または約10wt%以下の量が好ましい。便宜上、このグループの実施形態は、二つの水素化反応器を含む反応系に基づいて記載されるであろう。しかし、当業者は、容易に、いかに更なる反応器を反応系に加えることができるかを理解するであろう。
次の実施例は、バイオ成分原料を共処理することの問題を示す。この実施例においては、原料材を、商業的に入手可能なCoMo触媒により、水素化条件下に水素化する。図3は、得られた処理原料材の硫黄含有量に関するデータを示す。初めに、硫黄0.9wt%を含む鉱油留出油原料材を、647゜F(342℃)、全圧390psig、80%H2の処理ガス比1295scf/bbl、およびLHSV 0.3、で水素化した。図3に示されるように、鉱油原料の処理に対応する通油日数は、条件が硫黄含有量を10wppm以下へ低減するのに十分であったことを示す。57日目に、パーム油10wt%を、鉱油原料材へ添加した。処理ガス比をまた、パーム油の酸素含有量の増大に見合うように1480scf/bblへ増大した。これらの条件下に、処理原料材の硫黄含有量は、約100wppmの値へ急上昇した。反応器への原料を、単に鉱油留出油原料へ変更して戻した際には、得られた処理原料材の硫黄含有量は、10wppm未満へ降下した。いかなる特定の理論にも縛られることなく、パーム油における含酸素化合物の存在は、触媒活性の阻害をもたらし、処理原料材のより高い硫黄レベルをもたらすと考えられる。
バイオ成分原料材を共処理することの問題を克服するために、二段反応器が用いられることができる。第一段の条件は、実質的に全ての酸素を、バイオ成分原料から除去するように選択されることができ、一方原料材の硫黄は、管理可能なレベルへ低減される。図4は、示された反応器条件および処理される原料材のタイプに対して、得られた生成物の硫黄を示す。初めの処理条件には、温度621゜F(327℃)、圧力400psig、80%H2の水素流速度1100scf/bbl、および空間速度 1.0が含まれる。処理中の表示日数において、条件を、修正して、水素流速度が増大されるかまたは減少されるかのいずれか(1300scf/bbl、1700scf/bbl、または750scf/bblへ)、温度が昇温されるか(630゜F/332℃または640゜F/337℃へ)、若しくは鉱油原料材に含まれるパーム油の量が変更された。図4に示されるように、鉱油原料材は、硫黄0.9wt%を含む留出油原料材であった。バイオ成分は、硫黄を殆どまたは全く含まず、そのためにバイオ成分原料を鉱油留出油原料へ添加することは、硫黄含有量の低減をもたらしたことに注目されたい。
Claims (19)
- 低硫黄ディーゼル生成物を製造する方法であって、
T5沸点300゜F(149℃)以上を有し、かつ、鉱油部分および20wt%以下のバイオ成分部分を含む原料材を、第一の反応域に導入する工程;
前記原料材を、前記第一の反応域において、硫黄含有量2500wppm未満を有する第一の水素化原料材を製造するのに効果的な第一の水素化条件下に水素化する工程であって、前記原料材から酸素の少なくとも90wt%が除去される工程;
前記第一の水素化原料材を、蒸気ストリームおよび液体ストリームに分離する工程であって、蒸気部分は水素ガスを含む工程;
前記蒸気ストリームの少なくとも一部を、水素リサイクルループに送る工程;
前記液体ストリームの少なくとも一部を、第二の反応域へ送る工程;
前記第一の水素化原料材の液体部分を、前記第二の反応域において、硫黄含有量10wppm以下を有する水素化生成物を製造するのに効果的な第二の水素化条件下に水素化する工程;
前記水素化生成物を、蒸気生成物およびディーゼル沸点範囲生成物に分離する工程であって、前記蒸気生成物は、水素ガスを含む工程;
前記蒸気生成物の少なくとも一部を、前記水素リサイクルループに送る工程;
前記蒸気ストリームの部分および前記蒸気生成物の部分を、前記水素リサイクルループにおいて、CO除去系により処理する工程;および
前記水素リサイクルループからの水素を、水素処理ガスとして、前記第一の反応域に送る工程
を含むことを特徴とする方法。 - 前記CO除去系は、CO2スクラバーを含むことを特徴とする請求項1に記載の方法。
- 前記CO除去系は、アミンスクラバーおよび水性ガスシフト反応器であることを特徴とする請求項1に記載の方法。
- 前記バイオ成分原料材は、パーム油を含むことを特徴とする請求項1〜3のいずれかに記載の方法。
- 前記原料材の鉱油部分は、T95沸点775゜F(413℃)以下を有することを特徴とする請求項1〜4のいずれかに記載の方法。
- 前記原料材の鉱油部分は、常圧軽油、減圧軽油または軽質サイクル油であることを特徴とする請求項1〜5のいずれかに記載の方法。
- 前記ディーゼル沸点範囲生成物を水素異性化する工程を更に含むことを特徴とする請求項1〜6のいずれかに記載の方法。
- 前記原料材から酸素の少なくとも95wt%を除去することを特徴とする請求項1〜7のいずれかに記載の方法。
- 前記原料材から酸素の少なくとも98wt%を除去することを特徴とする請求項1〜8のいずれかに記載の方法。
- 前記第一の水素化原料材の酸素含有量は、0.1wt%以下であることを特徴とする請求項1〜9のいずれかに記載の方法。
- 前記第一の水素化原料材の酸素含有量は、0.05wt%以下であることを特徴とする請求項1〜10のいずれかに記載の方法。
- 前記第一の水素化原料材の酸素含有量は、0.01wt%以下であることを特徴とする請求項1〜11のいずれかに記載の方法。
- 前記効果的な第一の水素化条件は、LHSV0.5〜1.5、水素分圧100〜300psig(0.69〜2.07MPa)、少なくとも80%の水素(残りは不活性ガス)の水素処理ガス比650〜750scf/b(115.8〜133.6m 3 /m 3 )および温度500〜750゜F(260〜399℃)を含むことを特徴とする請求項1〜12のいずれかに記載の方法。
- 前記効果的な第一の水素化条件は、LHSV0.9〜1.1、水素分圧230〜270psig(1.59〜1.86MPa)、少なくとも80%の水素(残りは不活性ガス)の水素処理ガス比650〜750scf/b(115.8〜133.6m 3 /m 3 )および温度600〜650゜F(316〜343℃)を含むことを特徴とする請求項1〜13のいずれかに記載の方法。
- 前記効果的な第二の水素化条件は、LHSV0.5〜1.5、水素分圧250〜1500psig(1.72〜10.34MPa)、少なくとも95%の水素(残りは不活性ガス)の水素処理ガス比950〜1050scf/b(169.2〜187.0m 3 /m 3 )および温度550〜750゜F(288〜399℃)を含むことを特徴とする請求項1〜14のいずれかに記載の方法。
- 前記効果的な第二の水素化条件は、LHSV0.9〜1.1、水素分圧775〜925psig(5.34〜6.38MPa)、少なくとも95%の水素(残りは不活性ガス)の水素処理ガス比950〜1050scf/b(169.2〜187.0m 3 /m 3 )および温度625〜675゜F(329〜357℃)を含むことを特徴とする請求項1〜15のいずれかに記載の方法。
- 前記水素化生成物を水素異性化する工程を更に含むことを特徴とする請求項1〜16のいずれかに記載の方法。
- 前記導入される原料材の硫黄含有量は、0.25wt%以上であることを特徴とする請求項1〜17のいずれかに記載の方法。
- 前記導入される原料材の硫黄含有量は、2wt%以上であることを特徴とする請求項1〜18のいずれかに記載の方法。
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US8551327B2 (en) * | 2007-12-27 | 2013-10-08 | Exxonmobil Research And Engineering Company | Staged co-processing of biofeeds for manufacture of diesel range hydrocarbons |
US9279087B2 (en) * | 2008-06-30 | 2016-03-08 | Uop Llc | Multi-staged hydroprocessing process and system |
EP2362892B1 (en) | 2008-11-06 | 2019-04-17 | ExxonMobil Research and Engineering Company | Hydroprocessing of biodiesel fuels and blends |
US8785701B2 (en) | 2008-12-24 | 2014-07-22 | Exxonmobil Research And Engineering Company | Co-processing of diesel biofeed and kerosene range hydrocarbons |
WO2011031435A2 (en) * | 2009-08-28 | 2011-03-17 | Exxonmobil Research And Engineering Company | Reducing hydrogen consumption in hydrotreating of biocomponent feeds |
US8377288B2 (en) * | 2009-09-22 | 2013-02-19 | Bp Corporation North America Inc. | Methods and units for mitigation of carbon oxides during hydrotreating |
US20110099891A1 (en) * | 2009-11-04 | 2011-05-05 | Exxonmobil Research And Engineering Company | Hydroprocessing feedstock containing lipid material to produce transportation fuel |
JP5040986B2 (ja) * | 2009-12-10 | 2012-10-03 | 株式会社デンソー | 金属除去剤及び金属除去フィルタ |
ES2880706T3 (es) * | 2010-03-09 | 2021-11-25 | Exxonmobil Res & Eng Co | Desparafinado de combustible diésel renovable |
EP2545144B1 (en) * | 2010-03-09 | 2021-05-19 | ExxonMobil Research and Engineering Company | Hydroprocessing of diesel range biomolecules |
US9447350B2 (en) | 2010-10-29 | 2016-09-20 | Inaeris Technologies, Llc | Production of renewable bio-distillate |
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US20120053377A1 (en) | 2012-03-01 |
EP2240555A1 (en) | 2010-10-20 |
CN101925666A (zh) | 2010-12-22 |
JP2011508002A (ja) | 2011-03-10 |
AU2007362818A1 (en) | 2009-07-02 |
WO2009082366A1 (en) | 2009-07-02 |
CA2710276A1 (en) | 2009-07-02 |
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