JP6527470B2 - 酸化脱水素化装置を含むコンビナート - Google Patents
酸化脱水素化装置を含むコンビナート Download PDFInfo
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- JP6527470B2 JP6527470B2 JP2015560498A JP2015560498A JP6527470B2 JP 6527470 B2 JP6527470 B2 JP 6527470B2 JP 2015560498 A JP2015560498 A JP 2015560498A JP 2015560498 A JP2015560498 A JP 2015560498A JP 6527470 B2 JP6527470 B2 JP 6527470B2
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- ethylene
- ethane
- catalyst
- oxidative dehydrogenation
- oxygen
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- 229910052713 technetium Inorganic materials 0.000 description 1
- PORWMNRCUJJQNO-UHFFFAOYSA-N tellurium atom Chemical compound [Te] PORWMNRCUJJQNO-UHFFFAOYSA-N 0.000 description 1
- 125000005931 tert-butyloxycarbonyl group Chemical group [H]C([H])([H])C(OC(*)=O)(C([H])([H])[H])C([H])([H])[H] 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000007704 wet chemistry method Methods 0.000 description 1
- 229910001928 zirconium oxide Inorganic materials 0.000 description 1
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Description
i)以下の式の触媒であり:
NixAaBbDdOe
式中、xは0.1〜0.9の数、好ましくは、0.3〜0.9、更に好ましくは0.5〜0.85、最も好ましくは、0.6〜0.8であり;
aは0.04〜0.9の数であり;
bは0〜0.5の数であり;
dは0〜0.5の数であり;
eは触媒の原子価状態を満たす数であり;
AはTi、Ta、V、Nb、Hf、W、Y、Zn、Zr、SiおよびAlまたはそれらの混合物からなる群から選択され;
BはLa、Ce、Pr、Nd、Sm、Sb、Sn、Bi、Pb、Tl、In、Te、Cr、Mn、Mo、Fe、Co、Cu、Ru、Rh、Pd、Pt、Ag、Cd、Os、Ir、Au、Hgおよびそれらの混合物からなる群から選択され;
DはCa、K、Mg、Li、Na、Sr、Ba、Cs、およびRbおよびそれらの混合物からなる群から選択され;および
Oは酸素であり;および
ii)以下の式の触媒であり:
MofXgYhOi
式中、XはBa、Ca、Cr、Mn、Nb、Ta、Ti、Te、V、Wおよびそれらの混合物からなる群から選択され;
YはBi、Ce、Co、Cu、Fe、K、Mg、V、Ni、P、Pb、Sb、Si、Sn、Ti、U、およびそれらの混合物からなる群から選択され;
f=1;
gは0〜2であり;
h=0〜2、ただし、Co、Ni、Feおよびそれらの混合物のhの合計値が0.5未満であり;
iは触媒の原子価状態を満たす数であり;
iii)以下の式の触媒であり:
VxMoyNbzTemMenOp
式中、MeはTa、Ti、W、Hf、Zr、Sbおよびそれらの混合物からなる群から選択される金属であり;および
xは0.1〜3であり;
yは0.5〜1.5であり;
zは0.001〜3であり;
mは0.001〜5であり;
nは0〜2であり;
およびpは混合された酸化物触媒の原子価状態を満たす数であり;
iv)以下の式の触媒であり:
MoaVbNbcTeeOn
式中、a=1.0;b=0.05〜1.0、c=0.001〜1.0、e=0.001〜0.5、およびnは他の成分の酸化状態により決定され;
v)以下の式の触媒であり:
MoaVbXcYdZeMfOn
式中、Xは少なくともNbおよびTaのうちの1つであり;Yは少なくともSbおよびNiのうちの1つであり;Zは少なくともTe、Ga、Pd、W、BiおよびAlのうちの1つであり;Mは少なくともFe、Co、Cu、Cr、Ti、Ce、Zr、Mn、Pb、Mg、Sn、Pt、Si、La、K、AgおよびInのうちの1つであり;a=1.0(正規化);b=0.05〜1.0;c=0.001〜1.0;d=0.001〜1.0;e=0.001〜0.5;およびf=0.001〜0.3;およびnは他の成分の酸化状態により決定される。
および
式中、MはFe、Co、Ni、Cu、PdおよびPtからなる群から選択され;およびR1、R2、R3、R4、R5およびR6は、水素原子、ヘテロ環基、シアノ基、カルボン酸塩、カルボン酸エステル、ケト基、ニトロ基、ニトロ基、およびスルホニル基であるまたは含む電子吸引基、ヒドロカルビルラジカルが置換されていないまたは全部または一部置換された、好ましくはハロゲン原子によって置換されたC1-4アルキル基、C5-8アルキル基、C2-8アルケニル基およびC6-8アリール基からなる群から選択されるヒドロカルビルラジカルからなる群から独立して選択される。
本発明に係る使用されうる多くの触媒がある。以下の触媒システムは個別にまたは組み合わせて使用しうる。当業者は、組み合わせは、触媒の組み合わせが使用される場合、任意の拮抗作用があるかどうかを決定する実験室規模で試験する必要があることを理解するであろう。
i)以下の式の触媒であり:
NixAaBbDdOe
式中、xは0.1〜0.9の数、好ましくは、0.3〜0.9、更に好ましくは0.5〜0.85、最も好ましくは、0.6〜0.8であり;
aは0.04〜0.9の数であり;
bは0〜0.5の数であり;
dは0〜0.5の数であり;
eは触媒の原子価状態を満たす数であり;
AはTi、Ta、V、Nb、Hf、W、Y、Zn、Zr、SiおよびAlまたはそれらの混合物を含む群から選択され;
BはLa、Ce、Pr、Nd、Sm、Sb、Sn、Bi、Pb、Tl、In、Te、Cr、Mn、Mo、Fe、Co、Cu、Ru、Rh、Pd、Pt、Ag、Cd、Os、Ir、Au、Hgおよびそれらの混合物からなる群から選択され;
DはCa、K、Mg、Li、Na、Sr、Ba、Cs、およびRbおよびそれらの混合物からなる群から選択され;および
Oは酸素であり;および
ii)以下の式の触媒であり:
MofXgYhOi
式中、XはBa、Ca、Cr、Mn、Nb、Ta、Ti、Te、V、Wおよびそれらの混合物からなる群から選択され;
YはBi、Ce、Co、Cu、Fe、K、Mg、V、Ni、P、Pb、Sb、Si、Sn、Ti、U、およびそれらの混合物からなる群から選択され;
f=1;
gは0〜2であり;
hは0〜2、ただし、Co、Ni、Feおよびそれらの混合物のhの合計値が0.5未満であり;
iは触媒の原子価状態を満たす数であり;および
それらの混合物。
xは0.1〜3、好ましくは0.5〜2.0、さらに好ましくは0.75〜1.5であり;
yは0.5〜1.5、好ましくは0.75〜1.0であり;
zは0.001〜3、好ましくは0.1〜2、最も好ましくは0.5〜1.5であり;
mは0.001〜5、好ましくは1〜4であり;
nは0〜2であり、好ましくはnは0であり、しかし、Meが存在するとき、nは好ましくは0.5〜1.5であり、および
pは混合された酸化物触媒の原子価状態を満たす数である。
酸化脱水素化触媒を支持し得るいくつかの方法がある。
典型的に、担体上に充填する触媒は、前記触媒の0.1〜20重量%、通常、5〜15重量%、好ましくは8〜12重量%および前記担体の99.9〜80重量%、通常、85〜95重量%、好ましくは88〜92重量%を提供する。
上記のように、担体は、好ましくは50m2/g未満、より好ましくは20m2/g未満の低表面積を有しうる。担体は圧縮成形により製造されてよい。より高い圧力では、セラミック前駆体中の隙間が圧縮され崩壊すことがある。担体前駆体に加わる圧力に応じて、担体の表面積は約20〜10m2/gであってもよい。担体は多孔質となり、約0.1〜3.0ml/g、通常0.3〜1.0ml/gの細孔容量を有するだろう。セラミックの細孔サイズは小さくてもよい。好ましい細孔サイズ(直径)は約3〜10nmの範囲である。小さな孔径は膜を横切る圧力降下を維持するのに役立つようにセラミック膜で有用であるため、膜の破損は圧力の急激な変化により速やかに検出される。さらに、小さな孔径は、膜の全体の触媒化表面上の反応のより均一な分布を促進する。すなわち、より大きな孔が使用される場合、酸素の大部分は、酸素含有ガスは最初に接触するセラミック部分を通って拡散する傾向がある。セラミックの残りの部分は、主に使用されない。
酸化的脱水素化は、300℃〜550℃、通常は300℃〜500℃、好ましくは350℃〜450℃の温度で、0.5〜100psi(3.447〜689.47kPa)、好ましくは、15〜50psi(103.4〜344.73kPa)の圧力で実施されてもよく、反応器中のパラフィンの滞留時間は、通常、0.002〜30秒、好ましくは、1〜10秒である。エタンフィードは好ましくは95%、更に好ましくは98%の純度でるべきである。好ましくは、その工程は95%超え、好ましくは98%超えのオレフィン(エチレン)に対する選択性を有する。ガス毎時空間速度(GHVS)は500〜30000/時間、好ましくは、1000/時間であろう。触媒のキログラム当たりのグラム/時間でエチレン(生産性)の空時収率は、900以上、好ましくは1500超え、3000超え、最も好ましくは350〜400℃で3500超えであろう。触媒の生産性は、選択性が犠牲にされるまで、温度の上昇に伴って増加するであろうことに留意すべきである。
生成物エチレンストリームに同伴される酸素の量は更なる処理のために最小化されるべきである。しかし、生成物ストリーム中に酸素の一部少量が存在しうる。生成物ストリームの更なる処理の前に、酸素が生成物ストリームから除去されることが非常に望ましい。酸化脱水素化反応器のすぐ下流は、約3%を超えるエチレン生成物を消費することなく残留酸素を消費する低温度反応器であってもよい。この低温度反応器は、通常、Mn2O3とCuMn2O4の混合物である触媒を使用し、前記混合物は実験式Cu-MnxOpを有し、式中、xは0.1〜8であり、pは混合触媒の原子価状態を満たす数である。低温度酸素排除反応器は、400℃未満または400℃、通常は100℃〜400℃で操作する。前記低温度反応器の燃料は、パラフィン供給ストリーム中に加えたまたは存在する、あるいは残留酸素を消費するのに十分な量で酸化脱水素反応器からの生成物ストリームに加えられ得るいずれかであるメタン、水素、COおよびそれらの混合物からなる群から選択されてもよい。いくつかの実施形態において、時々アフターバーナーとして言及される脱酸素剤は、水洗、CO2除去、典型的なC2スプリッターまたはエタンからエチレンを分離する他の方法を含みうる生成物分離を含む多くの他の工程により続いてもよい。1つのそのような実施形態を図1に示す。
エチレンは、好ましくは、脱酸素剤と乾燥機を通過した後、エチレンとエタンを分離するために分解装置の下流のC2スプリッターに供給されうる。
および
式中、Mは、Fe、Co、Ni、Cu、PdおよびPtからなる群から選択され;およびR1、R2、R3、R4、R5およびR6は水素原子、ヘテロ環基、シアノ基、カルボン酸基、カルボン酸エステル、ケト基、ニトロ基およびスルホニル基またはそれらを含む電子吸引基、非置換または全部または一部置換された、好ましくは、ハロゲン原子で置換されたC1-4アルキル基、C5-8アルキル基 、C2-8アルケニル基およびC6-8アリール基からなる群から選択されるヒドロカルビルラジカルでからなる群から独立して選択される。イオン性液体は、非反応性溶媒または共溶媒とともに使用されてよい。溶媒は従来の芳香族溶媒、典型的には、トルエンの群から選択されてもよい。吸着圧力は、200psig〜300psig(1.3×103〜2×103kPag)、好ましくは250psig(1.7×103kPag)未満の範囲であってもよく、吸着温度は大気温度〜200℃、好ましくは150℃未満の範囲であってもよく、そしてオレフィンは少なくとも50psig(3.4×102kPa)の圧力を下げかつ15℃以上の温度上昇させることの1または2以上によるイオン性液体から放出されてよい。
コンビナートはさらに供給ストリームとしてエチレン、エタンまたはその両方を使用する1または2以上の単位操作を含んでもよい。
エチレンは重合化することができる。エチレンを重合化するための多くの既知の方法がある。
エチレンまたはエタンまたはそれらの混合物は、酸化され酢酸を生成し、更にエチレンと一緒に反応して酢酸エチルを生成し、次に酢酸ビニルに変換されてもよい。上記分離工程で回収されたエチレンは、酸素および/または1:0.1〜100または1:0〜150、しかし好ましくは担持触媒に存在する重量で1:0.1〜10の重量比など、重量比1:0.1〜250の水と一緒に酸化反応器に供給されてもよい。本発明のこの段階の酸化反応は、100〜400℃、通常140〜350℃の範囲の温度で、大気圧または超大気圧で、例えば、5〜27バール(50〜270kPa)範囲で、適切に実施されてもよい。このタイプの反応中のように使用され得る多くの触媒がある。通常、触媒は原子番号44〜47および77〜79を有する1または2以上の遷移金属を有するモリブデンおよびタングステンを含む。
今日、エチレンオキシドはエチレンを酸素(95%以上)で触媒上で酸化する主に直接酸化工程により製造され、通常、銀シリケートだが時々、元素銀がシリカ担体上で(またはシリカ担体と共沈殿させて)使用されてもよい。触媒は活性物質やコーキングを低減する化学物質を含んでもよい。反応は、100℃〜300℃、通常、140℃〜250℃、好ましくは200℃未満の温度で起こる。圧力は、約7psi(約50kPa)〜約300psi(約2.1×103kPa)であってもよい。約15psi(約104kPa)〜約100psi(6.9×102kPa)の圧力を使用することがさらに好ましい。通常、空間速度は、約10/時間〜約15000/時間の範囲であってもよい。好ましくは、空間速度は、約10/時間〜約6000/時間の範囲である。さらに好ましくは、空間速度は、約50/時間〜約3000/時間の範囲である。Bowmanに1989年7月4日に発行され、ダウケミカルカンパニー(Dow Chemicals Company)に譲渡された米国特許第4,845,253号が1つのそのような工程を開示し、その内容は参考として本明細書に記載される。
エチレンエポキシドは、多くの下流の誘導体のための中間体である。エチレンエポキシドは、アルカリハロゲン化物、四級アンモニウムハロゲン化物、および四級ホスホニウムハロゲン化物等の触媒の存在下、CO2と反応することによりエチレングリコールに変換され、エチレンカーボネートを生成しうる。エチレンカーボネートは、通常は塩基(Na2CO3)の存在下、カーボネートに対する水の重量比約2:1未満の水と反応させることによってエチレングリコールに変換されてもよい。
エチレンのエタノールへの気相直接水和は、通常はリン酸を含侵させた粘度、シリカまたはアルミナである多孔質基材である固体触媒上で実施されてもよい。この気相水和工程において、エチレンのモル当たり水約0.4〜0.8モルのモル比を提供するのが一般的である。いくつかの工程で、リン酸は、その工程中の触媒の損失を補うためにフィードに添加される。反応は、235℃〜250℃の温度、約700psi〜1200psi(4.2×103kPa〜8.2×103kPa)の圧力で実施されてもよい。
発酵性有機原料(例えば、サトウキビ)の十分な供給のある管轄において、エタノールは発酵、続いてエタンを生成するために例えば硫酸中で脱水素化することよって生成することは、当業者によって認識されるだろう。
コンビナートは、塩化ビニルまたは塩化エチレン(EDC)へのエチレンのハロゲン化のための単位操作を含むことができる。EDCは任意に酸素の存在下、直接ハロゲン化又はエチレンのオキシハロゲン化によって得られてもよい。直接ハロゲン化は、触媒(例えば、FeCl3)の存在下、エチレンとガス状のハロゲン化物(例えば、HCl)の反応により気相で行われてよい。これは、発熱反応であり、熱を反応器から除去する必要がある。オキシハロゲン化工程において、酸素と水はまた反応器中に存在し、触媒成分は、CuClである。
エチレンとエタンは低温蒸留により分離されてよい。低温蒸留を介してエチレンとエタンの分離の例の基本ケースは、図2で示される。この例において、C2スプリッターフィードは、1600KPaで60モル%のエチレンと40モル%のエタンを含む60%の蒸気画分の混合物である。その供給ストリームは、トレイはカラムの下列の先頭から番号が付けられた、おおよそトレイ60でカラムに入る。蒸留カラムは、示された例において80%のMurphreeトレイ効率で、約100のトレイを含む。カラムの圧力で、純粋なエチレンの飽和温度は−37℃であり、エタンの飽和温度は−16℃である。還流比は得られたエチレン蒸留純度99.95モル%とエタン底純度99.5モル%で、3.6である。オーバーヘッドコンデンサーは、完全にエチレン蒸留物を濃縮しそして還流し、そして35MWの熱負荷を必要とする。ケトル型リボイラーは28MWの熱負荷を必要とする。その基本ケースの例示的な工程を表1にまとめる。
この例において、酸化脱水素化装置とC2スプリッター操作をモデル化した。エチレン生成物純度は、少なくとも99.9モル%、さらに好ましくは99.95モル%に増加した。
この例において、酸化脱水素化技術は既存のC2スプリッターを除去するAspenTech Aspen Plus(登録商標)を使用してモデル化される(C2スプリッターの基本ケースの構成を図2に示す)。この例において、酸化脱水素化装置は少なくとも99.9モル%、さらに好ましくは99.95モル%にエチレンの純度を増加する。
図6の工程は、AspenTech Aspen Plus(登録商標)ソフトウェアを使用してモデル化し、統合されたシステムの動作を分析した。
この例において、図7の工程はAspenTech Aspen Plus(登録商標)を使用してモデル化された。
この例において、酸化脱水素化装置への供給ストリームは、水蒸気分解プラントでアセチレン水素化反応器からの生成物である。この場合、エタンはフィード中に存在し、少なくとも60%、好ましくは80%、より好ましくは99.5%の変換で脱水素化される。
この例において、酸化脱水素化装置への供給ストリームは、油精製機からエタン/エチレン混合ストリームであり、それはFCC、水素化分解および水素処理操作からの混合C2画分を含みうるが、それに限定されない。この混合物中のエチレン含有量は8体積%〜80体積%であることができる。この場合、エチレンはフィード中に存在し、少なくとも60%、好ましくは80%、より好ましくは99.5%の変換で脱水素化される。
この例において、脱水素化装置への供給ストリームは、オイルサンド/ビチューメンアップグレーダーからのエタン/エチレン混合ストリームであり、それは液体コーキング、遅延性コーキングおよび水素化分解操作からの混合C2画分を含みうるが、それに限定されない。この混合物中のエチレン含有量は、8体積%〜80体積%であることができる。この場合、エタンはフィード中に存在し、少なくとも60%、好ましくは80%、より好ましくは99.5%で脱水素化される。
本実施例において、膜反応器は膜チューブの束の膜からなり、触媒は、図9に示すように、チューブの内側に装填される。この反応器の設計は、反応器容器壁、触媒および膜材料との間の異なる熱膨張係数による膜チューブ損傷の可能性を減少する。内部反応器壁は、任意の潜在的な暴走反応の間、高温に耐えうるセラミックでコーティングされてもよい。
1.エタンは、余熱され、酸素は余熱されない。
2.酸素は余熱され、エタンは余熱されない。
3.エタンと酸素の両方が余熱される。
当該実施例において考えられた反応器の設計は、酸素が各および別々のチューブを通り膜に供給されることを除き、実施例10と同じであり、各膜は、独自の酸素チューブを有する。1つのチューブが損傷が破裂している場合、このオプションは、複数の膜チューブの損傷の可能性を減らすことができた。1つの膜が破れ、反応が起こっていない場合には、反応器はある方法で設計されなければならず、酸素レベルは、他の膜チューブからの反応生成物によって安全に希釈される。また、反応器の下流の分析装置は、生成物の酸素含有量中で増加を検出することができ、膜損傷の可能性の検査のためにすぐに反応器を停止する。
図11に示されるように多くのベッド反応器アプローチにおいて、酸素とエタンは予備混合流体または酸素のいずれかとして第1のベッドに供給され、エタンは反応器入り口で混合される。反応器は操作の動作の上昇流または下降流のモードのいずれかで操作できる。各触媒ベッドに供給される混合物中で酸素の濃度は、混合物はその上の爆発限界(UEL)の上であるようなものである。酸素の最大許容量は、暴走反応の場合に反応器中で最高許容温度に基づいて算出されてもよい。酸素は、重量平均ベッド温度以下の温度で供給され、急冷ガスとして働く。
本実施例において、2つの実験室規模の直列の触媒ベッドは、エタンの酸化脱水素化を立証るために使用されている。両触媒ベッドは、体積で0.2cm3である。第1の触媒ベッドは、281mgの触媒を加え、入り口ガス容積流量率は900cm3/hrであり、77.3モル%のエタンと22.3モル%の酸素で構成される。第2の触媒ベッドは、290mgの触媒が加えられ、第2の触媒ベッドの入り口ガスは、第1の触媒ベッドと300cm3/hrの酸素から生成物全体を構成する。第2の触媒ベッド入り口と出口の成分の質量流量率を表6にまとめる。
本発明は、エチレンへの生成物ストリーム中でエタンを変換し、分離トレーン上でエタンの負荷を軽減し協同する酸化脱水素化装置を組み込むことによって、エチレン分解装置の下流分離トレーンを完全に利用する低コストルートを提供することを目的とする。
Claims (14)
- 以下を含む化学コンビナート:
1)高圧ポリエチレン装置、ガス相ポリエチレン装置、スラリー相ポリエチレン装置、溶液相ポリエチレン装置、酢酸装置、酢酸ビニル装置、エチレンエポキシド装置、エチレングリコール装置、エタノール装置、エチレンジクロライド装置、エタノール脱水素化装置、および酢酸脱水素化装置からなる群から選択される1または2以上の装置;
および
2)C2極低温蒸留塔(極低温スプリッター)に大部分がエチレンおよびエタンからなる混合物を供給する水蒸気分解装置、および
前記C2極低温スプリッターと統合された、エチレンおよびエタンの混合ストリームにおけるエタンの酸化脱水素化のための酸化脱水素化装置、これは i)C2極低温蒸留塔からのボトムストリーム、または;
ii)C2極低温蒸留塔から下部トレイからの供給をとり、C2極低温蒸留塔中の上部トレイに生成物を戻すC2極低温蒸留塔からのストリーム、または;
iii)i)およびii)の両方を処理し;
ここで、エチレンへのエタンの酸化脱水素化は、250℃〜600℃の温度、0.5〜100psi(3.4〜689.5kPa)の圧力で実施され、以下からなる群から選択される触媒の存在下で毎時触媒1kg当たり1000g以上のエチレンの生産性を有する:
a)以下の式の触媒であり:
VxMoyNbzTemMenOp
式中、MeはTa、Ti、W、Hf、Zrおよびそれらの混合物からなる群から選択される金属であり;および
xは0.1〜3であり;
yは0.5〜1.5であり;
zは0.001〜3であり;
mは0.001〜5であり;
nは0〜2であり;
およびpは混合された酸化物触媒の原子価状態を満たす数であり;および
b)以下の式の触媒であり:
MoaVbNbcTeeO p
式中、a=1.0;b=0.05〜1.0、c=0.001〜1.0、e=0.001〜0.5、およびpは他の成分の酸化状態により決定される。 - 式a)の前記触媒中、nが0である、請求項1に記載の化学コンビナート。
- 酸化脱水素化装置は、エチレンを製造するために95%以上の選択性を有する、請求項1に記載の化学コンビナート。
- 酸化脱水素化触媒はチタン、ジルコニア、アルミニウム、マグネシウム、イットリア、ランタナ、シリカの酸化物およびそれらの混合組成物から選択される99.9〜80重量%の不活性多孔質セラミック膜を含み、前記触媒の0.1〜20重量%を供給する、請求項3に記載の化学コンビナート。
- 酸化脱水素化装置は、外殻とセラミックチューブの内部で酸素含有ガスの分離流路を画定する1または2以上の前記内部セラミックチューブと反応器の外壁とエチレン含有ガスの流路を画定するセラミックチューブの間の通路を含む、請求項4に記載の化学コンビナート。
- セラミックチューブはさらに内部スチールメッシュと外部スチールメッシュを含む、請求項5に記載の化学コンビナート。
- エチレンへのエタンの酸化脱水素化は300℃〜550℃の温度で実施される、請求項6に記載の化学コンビナート。
- エチレン塩化物装置が存在し、必要に応じて、酸素の存在下、エチレンを塩化物と反応させてエチレン塩化物を生成する、請求項6に記載のコンビナート。
- 酢酸装置が存在し、酸化脱水素化装置、水蒸気分解装置または両方からの1または2以上のエタンおよびエチレンを酸化し、酢酸を生成する、請求項6に記載のコンビナート。
- 酢酸装置からの酢酸はエチレンと反応して酢酸ビニルを生成する、請求項9に記載のコンビナート。
- 酸化脱水素化触媒は、チタン、ジルコニア、アルミニウム、マグネシウム、イットリア、ランタナ、シリカの酸化物およびそれらの混合組成物から選択される20〜5m2/gの表面積を有する99.9〜80重量%の不活性セラミックおよび0.1〜20重量%の前記触媒を含む、請求項3に記載の化学コンビナート。
- エチレン塩化物装置が存在し、必要に応じて、酸素の存在下、エチレンを塩化物と反応させてエチレン塩化物を生成する、請求項11に記載のコンビナート。
- 酢酸装置が存在し、酸化脱水素化工程、水蒸気分解装置または両方からの1または2以上のエタンおよびエチレンを酸化し、酢酸を生成する、請求項11に記載のコンビナート。
- 酢酸装置からの酢酸はエチレンと反応して酢酸ビニルを生成する、請求項13に記載のコンビナート。
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US9545610B2 (en) | 2017-01-17 |
KR102194118B1 (ko) | 2020-12-23 |
MX2019005606A (es) | 2019-08-12 |
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EP2964596A4 (en) | 2016-10-26 |
JP2016510731A (ja) | 2016-04-11 |
US9993798B2 (en) | 2018-06-12 |
CN109721459A (zh) | 2019-05-07 |
KR20150128720A (ko) | 2015-11-18 |
EP2964596A1 (en) | 2016-01-13 |
US20140249339A1 (en) | 2014-09-04 |
BR112015020073A2 (pt) | 2017-07-18 |
CA2840447A1 (en) | 2014-09-04 |
CN109721459B (zh) | 2022-05-27 |
US20180236432A1 (en) | 2018-08-23 |
MX2019005747A (es) | 2019-08-12 |
MX365705B (es) | 2019-06-11 |
CN105408291B (zh) | 2018-12-14 |
US10357754B2 (en) | 2019-07-23 |
WO2014134703A1 (en) | 2014-09-12 |
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