JP6273202B2 - 段間スチームストリッピングを伴う水素化分解法 - Google Patents
段間スチームストリッピングを伴う水素化分解法 Download PDFInfo
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- JP6273202B2 JP6273202B2 JP2014523068A JP2014523068A JP6273202B2 JP 6273202 B2 JP6273202 B2 JP 6273202B2 JP 2014523068 A JP2014523068 A JP 2014523068A JP 2014523068 A JP2014523068 A JP 2014523068A JP 6273202 B2 JP6273202 B2 JP 6273202B2
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/301—Boiling range
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4093—Catalyst stripping
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/80—Additives
- C10G2300/805—Water
- C10G2300/807—Steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
本願は、その内容が本明細書の一部を構成する米国仮出願第61/513,029号(出願日2011年7月29日)に基づく優先権を主張する。
本発明の好ましい態様は、以下を包含する。
[1]炭化水素原料を水素化分解するための方法であって、以下のステップ:
ヘテロ原子の除去および高分子量分子の低分子量炭化水素への水素化分解のための第1段リアクターの入口に原料を供給し、第1段リアクターストリームを製造し;その後
該第1段のエフルエントをスチームストリッパーベッセルへ送り、水素、H 2 S、NH 3 、軽質ガス(C1-C4)、ナフサおよび軽油を分離し;
ストリッパー塔底液を該ストリッパーベッセルから第2段リアクターへ送り;
第2段リアクターからの水素化分解されたエフルエントストリームを、水素、H 2 S、NH 3 、軽質ガス(C1-C4)、ナフサおよび軽油とを混合し、混合された生成物ストリームを形成し、そして
該混合された生成物ストリームを、構成成分を予め決められた製品ストリームに分離するための分離段階へと送る、
を含んでなる方法。
[2]第1段リアクターからのエフルエントストリームが、スチームストリッパーベッセルを通る前に、熱交換水蒸気発生器を通る、請求項1に記載の方法。
[3]第1段リアクターからのエフルエントストリームが、スチームストリッパーベッセルを通る前に、気液分離ストリッパーベッセルを通る、請求項1に記載の方法。
[4]第1段の水素化分解触媒が、アモルファス系アルミナ触媒、アモルファス系シリカアルミナ触媒、ゼオライト系触媒、並びにアモルファス系アルミナ触媒、アモルファス系シリカアルミナ触媒およびゼオライト系触媒の少なくとも1つを含む組合せ、からなる群から選択される、請求項1記載の方法。
[5]第1段の水素化分解触媒が、さらに、Ni、W、Mo、Co、またはNi、W、MoおよびCoの少なくとも1つを含む組合せの活性相を含んでなる、請求項1に記載の方法。
[6]100〜200 kg/cm 2 の範囲内の水素分圧で10〜80体積%の沸点370℃超の炭化水素が、沸点範囲180℃〜375℃のエタン、プロパン、n-ブタン、イソブテン、硫化水素、アンモニア、ナフサ留分、沸点範囲180℃〜375℃の軽油留分からなる群から選択される1以上の軽質ガスおよび該軽質ガスの少なくとも1つを含む組合せに変換される、請求項1記載の方法。
[7]水素分圧が100〜150 kg/cm 2 の範囲である、請求項1に記載の方法。
[8]原料油のストリームが、水素化処理触媒1000m 3 に対し1時間当たり300〜2000 m 3 の範囲である、請求項1に記載の方法。
[9]リアクターが、固定床、沸騰床、スラリー床、またはそれらの組み合わせである、請求項1に記載の方法。
[10]スチームストリッパーベッセルから取り出された水素、H 2 S、NH 3 、軽質ガス(C1-C4)、ナフサ、および軽油のエフルエントストリームの一部を、分離ベッセルに通して、水、ガスおよび液体に分離し、該分離ベッセルには中高硫黄(sour)軽油ストリームをさらに供給して該エフルエントストリームと混合し、該混合されたエフルエント/中高硫黄(sour)軽油ストリームを、軽油水素化処理ユニットに通して超低硫黄軽油を製造する、請求項1記載の方法。
Claims (10)
- 炭化水素原料を水素化分解するための方法であって、以下のステップ:
ヘテロ原子の除去および高分子量分子の低分子量炭化水素への水素化分解のための第1段リアクターの入口に原料を供給し、第1段リアクターエフルエントを製造し;その後
該第1段のエフルエントをスチームストリッパーベッセルへ送り、軽質ガス(C1-C4)、水素、H2S、NH 3 および名目上の沸点範囲36〜370℃の成分をストリッパー塔底液から分離し、前記名目上の沸点範囲36〜370℃の成分はナフサおよび軽油を含み;
ストリッパー塔底液を該ストリッパーベッセルから第2段リアクターへ送り;
第2段リアクターからの水素化分解されたエフルエントストリームを、スチームストリッパーベッセルにおいて分離された水素、H2S、NH3、軽質ガス(C1-C4)、名目上の沸点範囲36〜370℃の成分とを混合し、混合された生成物ストリームを形成し;、そして
該混合された生成物ストリームを、構成成分を予め決められた製品ストリームに分離するための分離段階へと送る、
を含んでなる方法。 - 第1段リアクターからのエフルエントストリームが、スチームストリッパーベッセルを通る前に、熱交換水蒸気発生器を通る、請求項1に記載の方法。
- 第1段リアクターからのエフルエントストリームが、気液分離ストリッパーベッセルを通り、塔底液および塔頂液を製造し、該塔底液をスチームストリッパーベッセルへ通過させる、請求項1に記載の方法。
- 第1段の水素化分解触媒が、アモルファス系アルミナ触媒、アモルファス系シリカアルミナ触媒、ゼオライト系触媒、並びにアモルファス系アルミナ触媒、アモルファス系シリカアルミナ触媒およびゼオライト系触媒の少なくとも1つを含む組合せ、からなる群から選択される、請求項1記載の方法。
- 第1段の水素化分解触媒が、さらに、Ni、W、Mo、Co、またはNi、W、MoおよびCoの少なくとも1つを含む組合せの活性相を含んでなる、請求項1に記載の方法。
- 100〜200 kg/cm2の範囲内の水素分圧で10〜80体積%の沸点370℃超の炭化水素が、沸点範囲180℃〜375℃のメタン、エタン、プロパン、n-ブタン、イソブテン、硫化水素、アンモニア、ナフサ留分、沸点範囲180℃〜375℃の軽油留分からなる群から選択される1以上の軽質ガスおよび該軽質ガスの少なくとも1つを含む組合せに変換される、請求項1記載の方法。
- 水素分圧が100〜150 kg/cm2の範囲である、請求項1に記載の方法。
- 原料油のストリームが、水素化処理触媒1000m3に対し1時間当たり300〜2000 m3の範囲である、請求項1に記載の方法。
- リアクターが、固定床、沸騰床、スラリー床、またはそれらの組み合わせである、請求項1に記載の方法。
- スチームストリッパーベッセルから取り出された水素、H2S、NH3、軽質ガス(C1-C4)、ナフサ、および軽油のエフルエントストリームの一部を、分離ベッセルに通して、水、ガスおよび液体に分離し、該分離ベッセルには中高硫黄(sour)軽油ストリームをさらに供給して該エフルエントストリームと混合し、該混合されたエフルエント/中高硫黄(sour)軽油ストリームを、軽油水素化処理ユニットに通して超低硫黄軽油を製造する、請求項1記載の方法。
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US201161513029P | 2011-07-29 | 2011-07-29 | |
US61/513,029 | 2011-07-29 | ||
PCT/US2012/048559 WO2013019624A1 (en) | 2011-07-29 | 2012-07-27 | Hydrocracking process with interstage steam stripping |
Publications (3)
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JP2014527100A JP2014527100A (ja) | 2014-10-09 |
JP2014527100A5 JP2014527100A5 (ja) | 2015-04-02 |
JP6273202B2 true JP6273202B2 (ja) | 2018-01-31 |
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JP2014523068A Active JP6273202B2 (ja) | 2011-07-29 | 2012-07-27 | 段間スチームストリッピングを伴う水素化分解法 |
Country Status (6)
Country | Link |
---|---|
US (1) | US9803148B2 (ja) |
EP (1) | EP2737027B1 (ja) |
JP (1) | JP6273202B2 (ja) |
KR (1) | KR101956407B1 (ja) |
CN (1) | CN104114679B (ja) |
WO (1) | WO2013019624A1 (ja) |
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US20090159493A1 (en) * | 2007-12-21 | 2009-06-25 | Chevron U.S.A. Inc. | Targeted hydrogenation hydrocracking |
US8173009B2 (en) | 2009-02-06 | 2012-05-08 | Uop Llc | Process for improving a hydrotreated stream |
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US20130098802A1 (en) | 2013-04-25 |
US9803148B2 (en) | 2017-10-31 |
KR101956407B1 (ko) | 2019-03-08 |
WO2013019624A9 (en) | 2013-09-19 |
WO2013019624A1 (en) | 2013-02-07 |
KR20140079763A (ko) | 2014-06-27 |
CN104114679A (zh) | 2014-10-22 |
CN104114679B (zh) | 2016-04-13 |
EP2737027A1 (en) | 2014-06-04 |
EP2737027B1 (en) | 2018-12-26 |
JP2014527100A (ja) | 2014-10-09 |
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