JP6907236B2 - 流体ストリームからc5〜c8−炭化水素及び酸性ガスを分離する方法 - Google Patents
流体ストリームからc5〜c8−炭化水素及び酸性ガスを分離する方法 Download PDFInfo
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- JP6907236B2 JP6907236B2 JP2018560244A JP2018560244A JP6907236B2 JP 6907236 B2 JP6907236 B2 JP 6907236B2 JP 2018560244 A JP2018560244 A JP 2018560244A JP 2018560244 A JP2018560244 A JP 2018560244A JP 6907236 B2 JP6907236 B2 JP 6907236B2
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- acid gas
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Classifications
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1487—Removing organic compounds
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D—SEPARATION
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- B—PERFORMING OPERATIONS; TRANSPORTING
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Description
a) 流体ストリームを、少なくとも1種のアミンを含む吸収媒体と吸収区域で接触させて、脱酸された流体ストリーム及び酸性ガス取り込み済み吸収媒体を得、
b) 前記取り込み済み吸収媒体を第1の熱交換器で加熱し、減圧区域内に5〜10バールの圧力まで減圧して、C5〜C8−炭化水素含有気相及び炭化水素を除去した取り込み済み吸収媒体を得、
c) 炭化水素を除去した取り込み済み吸収媒体をストリッパーに通し、ストリッパー内で1〜2.5バールの圧力で酸性ガスを熱供給によって少なくとも部分的に遊離させて、再生された吸収媒体と酸性ガス含有ストリームを得、炭化水素を除去した取り込み済み吸収媒体は、ストリッパーに導入する前に第2の熱交換器で任意に加熱し、
d) 再生された吸収媒体を吸収区域内へ再循環させる
方法によって達成される。
第2の熱交換器が存在する場合、第2の熱交換器で使用する熱媒体は再生された吸収媒体であり、第1の熱交換器で使用する熱媒体は第2の熱交換器を通過した後の再生された吸収媒体であり、又は第2の熱交換器が存在しない場合は、第1の熱交換器で使用する熱媒体は再生された吸収媒体であり、
第1の熱交換器で伝達される熱量は、C5〜C8−炭化水素含有気相が、50体積%〜97体積%の酸性ガスを、好ましくは70体積%〜95体積%の酸性ガスを、例えば80体積%〜95体積%の酸性ガスを含むような量である。
(i) 式I:
NR1(R2)2 (I)
(式中、R1は、C2〜C6−ヒドロキシアルキル基、C1〜C6−アルコキシ−C2〜C6−アルキル基、ヒドロキシ−C1〜C6−アルコキシ−C2〜C6−アルキル基及び1−ピペラジニル−C2〜C6−アルキル基から選択され、R2は、H、C1〜C6−アルキル基及びC2〜C6−ヒドロキシアルキル基から独立して選択される)のアミン;
(ii) 式II:
R3R4N−X−NR5R6 (II)
(式中、R3、R4、R5及びR6は、H、C1〜C6−アルキル基、C2〜C6−ヒドロキシアルキル基、C1〜C6−アルコキシ−C2〜C6−アルキル基及びC2〜C6−アミノアルキル基から互いに独立して選択され、Xは、C2〜C6−アルキレン基、−X1−NR7−X2−又は−X1−O−X2−を表し、このX1及びX2は、互いに独立してC2〜C6アルキレン基を表し、R7は、H、C1〜C6−アルキル基、C2〜C6−ヒドロキシアルキル基又はC2〜C6−アミノアルキル基を表す)のアミン;
(iii) 環中に少なくとも1個の窒素原子を有し、環中に窒素及び酸素から選択される1個又は2個のさらなるヘテロ原子を含み得る5〜7員飽和複素環式化合物、及び
(iv) それらの混合物。
(i) 2−アミノエタノール(モノエタノールアミン)、2−(メチルアミノ)エタノール、2−(エチルアミノ)エタノール、2−(n−ブチルアミノ)エタノール、2−アミノ−2−メチルプロパノール、N−(2−アミノエチル)ピペラジン、メチルジエタノールアミン、エチルジエタノールアミン、ジメチルアミノプロパノール、t−ブチルアミノエトキシエタノール、2−アミノ−2−メチルプロパノール;
(ii) 3−メチルアミノプロピルアミン、エチレンジアミン、ジエチレントリアミン、トリエチレンテトラアミン、2,2−ジメチル−1,3−ジアミノプロパン、ヘキサメチレンジアミン、1,4−ジアミノブタン、3,3−イミノビスプロピルアミン、トリス(2−アミノエチル)アミン、ビス(3−ジメチルアミノプロピル)アミン、テトラメチルヘキサメチレンジアミン;
(iii) ピペラジン、2−メチルピペラジン、N−メチルピペラジン、1−ヒドロキシエチルピペラジン、1,4−ビスヒドロキシエチルピペラジン、4−ヒドロキシエチルピペラジン、ホモピペラジン、ピペリジン、2−ヒドロキシエチルピペリジン及びモルホリン;及び
(iv) それらの混合物、である。
アルカノールアミン、例えばモノエタノールアミン(MEA)、ジエタノールアミン(DEA)、エチルアミノエタノール、1−アミノ−2−メチルプロパン−2−オール、2−アミノ−1−ブタノール、2−(2−アミノエトキシ)エタノール及び2−(2−アミノエトキシ)エタンアミン、
ポリアミン、例えばヘキサメチレンジアミン、1,4−ジアミノブタン、1,3−ジアミノプロパン、3−(メチルアミノ)プロピルアミン(MAPA)、N−(2−ヒドロキシエチル)エチレンジアミン、3−(ジメチルアミノ)プロピルアミン(DMAPA)、3−(ジエチルアミノ)プロピルアミン、N,N’−ビス(2−ヒドロキシエチル)エチレンジアミン、
環中に少なくとも1個のNH基を有し、環中に窒素及び酸素から選択される1個又は2個のさらなるヘテロ原子を含み得る5員、6員又は7員飽和複素環式化合物、例えばピペラジン、2−メチルピペラジン、N−メチルピペラジン、N−エチルピペラジン、N−(2−ヒドロキシエチル)ピペラジン、N−(2−アミノエチル)ピペラジン、ホモピペラジン、ピペリジン及びモルホリン、
から選択される。
(i)水素含有流体ストリーム;これには、例えば、石炭ガス化又は水蒸気改質によって製造可能な合成ガスが含まれ、これらは任意に水性ガス転化反応に供される。この合成ガスは、例えばアンモニア、メタノール、ホルムアルデヒド、酢酸、尿素の製造用に、フィッシャー・トロプシュ合成に、又は石炭ガス化複合発電(IGCC)プロセスでのエネルギー生成に使用される。
cpaは、吸収区域内に通した吸収媒体の比熱容量であり、
cpfは、供給した流体ストリームの比熱容量である。
実施例の流体ストリーム1の組成、流速、温度及び圧力は、以下の通りであった:
2.0000体積%の CO2
0.0004体積%の H2S
1.0000体積%の N2
92.9796体積%の CH4
2.0000体積%の C2H6
1.0000体積%の C3H8
1.0000体積%の C6H14
0.0050体積%の ベンゼン
0.0050体積%の トルエン
0.0050体積%の エチルベンゼン
0.0050体積%の o−キシレン
流速(乾燥): 500000 m3(STP)/h
流速(水): 74 m3(STP)/h
流速(全体): 500074 m3(STP)/h
流速(全体): 401605 kg/h
温度: 30.0°C 圧力: 66.0 バール 本文書で報告するすべての圧力は絶対圧である。
図1によるプラントで方法の1つをシミュレートした。酸性ガスを取り込んだ吸収媒体をフラッシュタンク5内に6.2バールの圧力まで減圧した。ストリーム16を介して排出した気相及びフラッシュタンクから下方向に排出した吸収媒体の両方の温度は、34.6℃であった。ストリッパー7を1.7バールの圧力で操作した。新鮮な水1.87t/hを導管18を介して供給した。
図2によるプラントで方法の1つをシミュレートした。酸性ガスを取り込んだ吸収媒体をフラッシュタンク5内に6.2バールの圧力まで減圧した。ストリーム16を介して排出した気相及びフラッシュタンクから下方向に排出した吸収媒体の両方の温度は、95.8℃であった。ストリッパーを1.7バールの圧力で操作した。新鮮な水1.95t/hを導管18を介して供給した。
図3によるプラントで方法の1つをシミュレートした。酸性ガスを取り込んだ吸収媒体をフラッシュタンク5内に6.2バールの圧力まで減圧した。ストリーム16を介して排出した気相及びフラッシュタンクから下方向に排出した吸収媒体の両方の温度は、34.6℃であった。低圧フラッシュタンクを1.7バールの圧力で、ストリッパーを1.8バールの圧力で操作した。新鮮な水1.86t/hを導管18を介して供給した。
図4によるプラントで方法の1つをシミュレートした。酸性ガスを取り込んだ吸収媒体をフラッシュタンク5内に6.2バールの圧力まで減圧した。ストリーム16を介して排出した気相及びフラッシュタンクから下方向に排出した吸収媒体の両方の温度は95.8℃であった。低圧フラッシュタンクを1.7バールの圧力で、ストリッパーを1.8バールの圧力で操作した。新鮮な水1.94t/hを導管18を介して供給した。
**:この冷却器/熱交換器は、方法の実際の実施時には省略されるであろう。
Claims (15)
- 流体ストリームからC5〜C8−炭化水素及び酸性ガスを分離する方法であって、
a) 前記流体ストリームを、少なくとも1種のアミンを含む吸収媒体と吸収区域で接触させて、脱酸された流体ストリーム、及び酸性ガス取り込み済み吸収媒体を得、
b) 前記取り込み済み吸収媒体を第1の熱交換器で加熱し、減圧区域内で0.5〜1MPa(5〜10バール)の圧力まで減圧して、C5〜C8−炭化水素含有気相、及び炭化水素を除去した取り込み済み吸収媒体を得、
c) 前記炭化水素を除去した取り込み済み吸収媒体をストリッパーに通し、前記ストリッパー内で0.1〜0.25MPa(1〜2.5バール)の圧力で前記酸性ガスを熱供給によって少なくとも部分的に遊離させて、再生された吸収媒体と酸性ガス含有ストリームを得、前記炭化水素を除去した取り込み済み吸収媒体は、前記ストリッパーに導入する前に第2の熱交換器で加熱し、
d) 前記再生された吸収媒体を前記吸収区域内へ再循環させ、
ここで、
前記第2の熱交換器で使用する熱媒体は前記再生された吸収媒体であり、前記第1の熱交換器で使用する熱媒体は前記第2の熱交換器を通過した後の前記再生された吸収媒体であり、
前記第1の熱交換器で伝達される熱量は、前記C5〜C8−炭化水素含有気相が50体積%〜97体積%の酸性ガスを含むような量である方法。 - 前記第2の熱交換器での加熱の前に、前記炭化水素を除去した取り込み済み吸収媒体を、0.1〜0.25MPa(1〜2.5バール)の圧力まで脱着区域内で減圧し、前記酸性ガス含有ストリームとの直接熱交換によって予熱する、請求項1に記載の方法。
- 工程a)で、前記流体ストリームの、吸収区域での前記吸収媒体との接触は、5〜8MPa(50〜80バール)の圧力で行われる、請求項1又は2に記載の方法。
- 供給される前記流体ストリーム中の前記酸性ガスの分圧が0.1MPa(1バール)未満である、請求項1から3のいずれか一項に記載の方法。
- 供給される前記流体ストリーム中の前記酸性ガスの体積分率が3.3体積%未満である、請求項1から4のいずれか一項に記載の方法。
- 供給される前記流体ストリームの温度が70℃未満である、請求項1から5のいずれか一項に記載の方法。
- 前記C5〜C8−炭化水素含有気相が70〜95体積%の酸性ガスを含む、請求項1から6のいずれか一項に記載の方法。
- 前記第1の熱交換器で加熱した前記取り込み済み吸収媒体が、>0.6〜1MPa(>6〜10バール)の圧力まで前記減圧区域内で減圧される、請求項1から7のいずれか一項に記載の方法。
- 前記C5〜C8−炭化水素を前記C5〜C8−炭化水素含有気相から少なくとも部分的に凝縮させ、未凝縮成分を前記吸収区域内に通す請求項1から8のいずれか一項に記載の方法。
- 前記C5〜C8−炭化水素が、ベンゼン、トルエン、エチルベンゼン及びキシレンから選択される芳香族炭化水素を含む、請求項1から9のいずれか一項に記載の方法。
- 供給される前記流体ストリームが、0.5体積%〜10体積%の酸性ガス、及び10〜5000ppmvのC5〜C8−炭化水素を含む流体ストリームから選択される、請求項1から10のいずれか一項に記載の方法。
- 供給される前記流体ストリームが天然ガスである、請求項1から11のいずれか一項に記載の方法。
- 前記アミンが立体障害アミン又は第三級アミンである、請求項1から13のいずれか一項に記載の方法。
- 前記吸収媒体が立体障害のない第一級又は第二級アミンをさらに含む、請求項14に記載の方法。
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US4184855A (en) * | 1977-12-29 | 1980-01-22 | Union Carbide Corporation | Process for CO2 removal |
CA1205276A (en) * | 1981-06-15 | 1986-06-03 | Malcolm W. Mcewan | Process for the removal of co.sub.2 and, if present h.sub.2s from a gas mixture |
US6607585B2 (en) | 1997-02-11 | 2003-08-19 | David Morrow | Raw natural gas processing system and method of processing raw natural gas |
US6605138B2 (en) | 1999-04-21 | 2003-08-12 | Matthew T. Frondorf | Apparatus and method for exclusively removing VOC from regeneratable solvent in a gas sweetening system |
FR2898284B1 (fr) * | 2006-03-10 | 2009-06-05 | Inst Francais Du Petrole | Procede de desacidification d'un gaz par solution absorbante avec regeneration fractionnee par chauffage. |
FR2936165B1 (fr) * | 2008-09-23 | 2011-04-08 | Inst Francais Du Petrole | Procede de desacidification d'un gaz par solution absorbante avec controle de la demixtion |
BR112015004743A2 (pt) | 2012-09-05 | 2017-07-04 | Basf Se | processo para separação de gases ácidos de uma corrente de fluido que compreende água |
FR3006912B1 (fr) | 2013-06-14 | 2016-07-08 | Ifp Energies Now | Procede de decarbonatation d'un gaz hydrocarbone |
FR3020965B1 (fr) * | 2014-05-16 | 2016-05-27 | Ifp Energies Now | Solution absorbante a base de diamines tertiaires beta hydroxylees et procede d'elimination de composes acides d'un effluent gazeux |
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- 2017-02-02 RU RU2018132033A patent/RU2739735C9/ru active
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RU2018132033A3 (ja) | 2020-06-09 |
RU2018132033A (ru) | 2020-03-11 |
RU2739735C9 (ru) | 2021-06-25 |
AU2017217911A1 (en) | 2018-08-02 |
AU2017217911B2 (en) | 2021-10-07 |
US20190039013A1 (en) | 2019-02-07 |
EP3413996A1 (de) | 2018-12-19 |
US10864477B2 (en) | 2020-12-15 |
EP3413996B1 (de) | 2019-12-04 |
JP2019511362A (ja) | 2019-04-25 |
EP3628393A1 (de) | 2020-04-01 |
CA3013526A1 (en) | 2017-08-17 |
EP3628393B1 (de) | 2021-05-26 |
RU2739735C2 (ru) | 2020-12-28 |
MY186866A (en) | 2021-08-26 |
WO2017137309A1 (de) | 2017-08-17 |
CA3013526C (en) | 2023-10-17 |
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