JP2011524913A - エチルベンゼンのスチレンへの脱水素化のための二酸化炭素及び酸素の併用法 - Google Patents
エチルベンゼンのスチレンへの脱水素化のための二酸化炭素及び酸素の併用法 Download PDFInfo
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- JP2011524913A JP2011524913A JP2011514722A JP2011514722A JP2011524913A JP 2011524913 A JP2011524913 A JP 2011524913A JP 2011514722 A JP2011514722 A JP 2011514722A JP 2011514722 A JP2011514722 A JP 2011514722A JP 2011524913 A JP2011524913 A JP 2011524913A
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Abstract
Description
EB+CO2=スチレン+CO+H2O (CO2-ODH;吸熱)
EB+1/2O2→スチレン+H2O (O2-ODH;発熱)
CO2+H2=CO+H2O (水−ガスシフト;少量の反応熱のみ)
H2+1/2O2→H2O (発熱)
CO+1/2O2→CO2 (発熱)
O2の少量が炭化水素を燃焼することもある(発熱;望ましくない)。
直接脱水素化(O2又はCO2のいずれも使用しない)、
CO2-ODH(O2無し)又は
O2-ODH(希釈剤以外の有効な役割を果たすCO2無し)
のいずれかを使用する脱水素化セクションの下流での、組み合わせCO2/O2-ODH反応セクションの利用を含むものである。
Claims (17)
- 炭化水素供給原料を酸化脱水素化する方法であって、
(a)炭化水素供給原料を、炭化水素を脱水素化する酸化脱水素化反応器システムに供給する工程、ここで、脱水素化反応器は、炭化水素供給原料を選択的に酸化して、脱水素化炭化水素生成物を生成する少なくとも1の触媒を収容するものであり;
(b)二酸化炭素を酸化脱水素化反応器システムに供給する工程、ここで、二酸化炭素/総炭化水素供給原料(新鮮な供給物+再循環物)のモル供給比率が0.1〜10であり;
(c)酸素を酸化脱水素化反応器システムに供給する工程、ここで、酸素/総炭化水素供給原料(新鮮な供給物+再循環物)のモル供給比率が0.01〜1.0であり;
(d)炭化水素供給原料を、触媒脱水素化して、脱水素化炭化水素生成物、未反応炭化水素供給原料、副生物及びオフガスを含んでなる脱水素化生成物ストリームを生成する工程;及び
(e)脱水素化炭化水素生成物、未反応供給原料、副生物及びオフガスを回収する工程
を含んでなる、炭化水素供給原料の酸化脱水素化法。 - 脱水素化炭化水素生成物、未反応供給原料、副生物及びオフガスを回収する工程が、
(f)炭化水素化生成物ストリームを、凝縮システム及び分離システムを含んでなる主分離セクションに供給する工程;及び
(g)凝縮システムにおいて、脱水素化生成物ストリームの少なくとも一部を冷却及び凝縮し;及び分離システムにおいて、脱水素化生成物ストリームから、未反応炭化水素供給原料、凝縮した副生物及びオフガスを分離する工程
を含んでなるものである、請求項1記載の方法。 - さらに、未反応炭化水素供給原料を酸化脱水素化反応器システムに供給する工程を含んでなる、請求項2記載の方法。
- 炭化水素供給原料がパラフィンであり、脱水素化炭化水素生成物がオレフィンである、請求項1記載の方法。
- 炭化水素供給原料がエチルベンゼンであり、脱水素化炭化水素生成物がスチレンである、請求項1記載の方法。
- 二酸化炭素/エチルベンゼンのモル供給比率が0.3〜8であり、酸素/エチルベンゼンのモル供給比率が0.02〜0.6である、請求項5記載の方法。
- 酸化脱水素化反応器システムが、酸素選択膜補助脱水素化反応器を含むものである、請求項1記載の方法。
- 酸化脱水素化反応器システムが、流動床反応器システムを含むものである、請求項1記載の方法。
- 酸化脱水素化反応器システムが、反応混合物を再加熱/予熱するためのO2-ODH反応器を含むものである、請求項1記載の方法。
- 酸素を空気によって供給する、請求項1記載の方法。
- さらに、
(h)オフガスをコンプレッサーに供給する工程、ここで、オフガスは一酸化炭素を含んでなり、コプレッサーからの生成物が、一酸化炭素を含んでなる圧縮されたガスであり;
(i)圧縮されたガスを、一酸化炭素を二酸化炭素に転化する酸化器に供給する工程、ここで、酸化器からの生成物が二酸化炭素を含んでなり;
(j)酸化器から二酸化炭素を回収する工程;及び
(k)回収した二酸化炭素を酸化脱水素化反応器に再循環する工程
を含んでなる、請求項2記載の方法。 - さらに、
(h)オフガスをコンプレッサーに供給する工程、ここで、オフガスは、二酸化炭素及び一酸化炭素を含んでなり、コプレッサーからの生成物が、一酸化炭素及び二酸化炭素を含んでなる圧縮されたガスであり;
(i)圧縮されたガスを、オフガス中の二酸化炭素及び一酸化炭素を分離するセパレーターに供給して、一酸化炭素を含んでなるストリーム及び二酸化炭素を含んでなるストリームを生成する工程;
(j)一酸化炭素ストリームを、一酸化炭素を二酸化炭素に転化する酸化器に供給する工程、ここで、酸化器からの生成物が二酸化炭素を含んでなり;
(k)酸化器から二酸化炭素を回収する工程;及び
(l)回収した二酸化炭素を反応器に再循環する工程
を含んでなる、請求項2記載の方法。 - さらに、
(h)オフガスをコンプレッサーに供給する工程、ここで、オフガスは一酸化炭素を含んでなり、コプレッサーからの生成物が、一酸化炭素を含んでなる圧縮されたガスであり;
(i)圧縮されたガスを、一酸化炭素を二酸化炭素へ転化する水−ガスシフトユニットに供給する工程、ここで、水−ガスシフトユニットからの生成物が、二酸化炭素を含んでなる転化されたガスであり;
(j)転化されたガスを、転化されたガス中の二酸化炭素を分離するセパレーターに供給する工程、ここで、セパレーターからの生成物が二酸化炭素を含んでなり、
(k)セパレーターから二酸化炭素を回収する工程;及び
(l)回収した二酸化炭素を反応器に再循環する工程
を含んでなる、請求項2記載の方法。 - さらに、
(h)オフガスを、二酸化炭素を分離する吸収器/吸着器に供給する工程、ここで、オフガスは二酸化炭素を含んでなり、吸収器/吸着器からの生成物が二酸化炭素を含んでなり;
(i)吸収器/吸着器から二酸化炭素を回収する工程;及び
(j)回収した二酸化炭素を反応器に再循環する工程
を含んでなる、請求項2記載の方法。 - さらに、
(h)オフガスを、一酸化炭素から二酸化炭素を分離する吸収器/吸着器に供給する工程、ここで、オフガスは二酸化炭素及び一酸化炭素を含んでなり、吸収器/吸着器からの生成物が二酸化炭素を含んでなり、及び吸収器/吸着器からの副生物が一酸化炭素を含んでなり;
(i)副生物を、一酸化炭素を分離するセパレーターに供給する工程、ここで、セパレーターからの生成物が、一酸化炭素を含んでなる分離されたガスであり、
吸収器/吸着器から二酸化炭素を回収する工程;及び
(j)分離されたガスを、一酸化炭素を二酸化炭素に転化する酸化器に供給する工程、ここで、酸化器からの生成物が二酸化炭素を含んでなり;
(k)吸収器/吸着器及び酸化器から二酸化炭素を回収する工程;及び
(l)回収した二酸化炭素を反応器に再循環する工程
を含んでなる、請求項2記載の方法。 - さらに、
(h)オフガスを、一酸化炭素から二酸化炭素を分離する吸収器/吸着器に供給する工程、ここで、オフガスは二酸化炭素及び一酸化炭素を含んでなり、吸収器/吸着器からの生成物が二酸化炭素を含んでなり、及び吸収器/吸着器からの副生物が一酸化炭素を含んでなり;
(i)副生物を、一酸化炭素を二酸化炭素へ転化する水−ガスシフトユニットに供給する工程、ここで、水−ガスシフトユニットからの生成物が、二酸化炭素を含んでなる転化されたガスであり;
(j)転化されたガスを、転化されたガス中の二酸化炭素を分離するセパレーターに供給する工程、ここで、セパレーターからの生成物が二酸化炭素を含んでなり、
(k)吸収器/吸着器及びセパレーターから二酸化炭素を回収する工程;及び
(l)回収した二酸化炭素を反応器に再循環する工程
を含んでなる、請求項2記載の方法。 - さらに、
(h)オフガスを、一酸化炭素から二酸化炭素を分離する吸収器/吸着器に供給する工程、ここで、オフガスは二酸化炭素及び一酸化炭素を含んでなり、吸収器/吸着器からの生成物が二酸化炭素を含んでなり、及び吸収器/吸着器からの副生物が一酸化炭素を含んでなり;
(i)副生物を、一酸化炭素を分離するセパレーターに供給する工程、ここで、セパレーターからの生成物が、一酸化炭素を含んでなる分離されたガスであり、
(j)分離されたガスを、一酸化炭素を二酸化炭素へ転化する水−ガスシフトユニットに供給する工程、ここで、水−ガスシフトユニットからの生成物が、二酸化炭素を含んでなる転化されたガスであり;
(k)転化されたガスを、転化されたガス中の二酸化炭素を分離するセパレーターに供給する工程、ここで、セパレーターからの生成物が二酸化炭素を含んでなり、
(l)吸収器/吸着器及びセパレーターから二酸化炭素を回収する工程;及び
(m)回収した二酸化炭素を反応器に再循環する工程
を含んでなる、請求項2記載の方法。
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CN104677053A (zh) * | 2015-01-30 | 2015-06-03 | 北方华锦化学工业集团有限公司 | 一种回收乙苯脱氢尾气中氢气的方法 |
JP2020532540A (ja) * | 2017-08-28 | 2020-11-12 | 8 リバーズ キャピタル,エルエルシー | 二酸化炭素を使用するエタンの酸化脱水素 |
JP7216077B2 (ja) | 2017-08-28 | 2023-01-31 | 8 リバーズ キャピタル,エルエルシー | 二酸化炭素を使用するエタンの酸化脱水素 |
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SG192420A1 (en) | 2013-08-30 |
US20120294776A1 (en) | 2012-11-22 |
BRPI0915723A2 (pt) | 2015-10-27 |
CA2727286A1 (en) | 2009-12-23 |
KR20110033229A (ko) | 2011-03-30 |
TW201000438A (en) | 2010-01-01 |
AR074153A1 (es) | 2010-12-29 |
TW201247619A (en) | 2012-12-01 |
EP2303812A4 (en) | 2012-10-31 |
EP2303812A1 (en) | 2011-04-06 |
WO2009155219A1 (en) | 2009-12-23 |
US8765082B2 (en) | 2014-07-01 |
US8237000B2 (en) | 2012-08-07 |
ZA201100417B (en) | 2011-10-26 |
CN102159524A (zh) | 2011-08-17 |
CL2009001427A1 (es) | 2010-01-04 |
MX2010013804A (es) | 2011-03-21 |
TWI421238B (zh) | 2014-01-01 |
US20090318743A1 (en) | 2009-12-24 |
TWI439449B (zh) | 2014-06-01 |
NO20101712A1 (no) | 2011-01-04 |
SG192418A1 (en) | 2013-08-30 |
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