JP2017509745A5

JP2017509745A5 -

Info

Publication number: JP2017509745A5
Application number: JP2016553574A
Authority: JP
Filing date: 2014-12-23
Publication date: 2017-11-30
Anticipated expiration: 2034-12-23

Description

米国特許出願第２００７／０６２８４８号は、最大２個のＣ１−４アルキル基で置換されているまたは未置換の、少なくとも２個の縮合芳香環を含む少なくとも２０質量％の１つまたは複数の芳香族化合物を含む供給物を水素化分解して、少なくとも３５質量％のＣ２−４アルカン混合物を含む生成物流を製造するステップに関する。米国特許出願第２００７／０６２８４８号では、オイルサンドからのビチューメンは従来の蒸留装置に供給され、蒸留装置からのナフサ流はナフサ水素化処理装置に供給される。オーバーヘッドガス流は軽質ガス／軽質パラフィン流であり、炭化水素分解装置に供給される。蒸留装置からのディーゼル流はディーゼル水素化処理装置に供給され、蒸留装置からの軽油流は減圧蒸留装置に供給され、減圧蒸留装置からの減圧軽油流は軽油水素化処理装置に供給される。軽油水素化処理装置からの軽質ガス流は炭化水素分解装置に供給される。減圧軽油水素化処理装置からの水素化処理された減圧軽油は接触分解装置に供給される。減圧蒸留装置からの底部流は減圧（重質）残留物であり、ナフサ水素化処理装置に送られるナフサ流などの多くの流れを生成する重質油熱分解装置に送られ、ディーゼル流はディーゼル水素化処理装置に送られて水素化処理されたディーゼルが生成され、軽油流は減圧軽油水素化処理装置に供給されて、接触分解装置に供給される水素化処理された軽油流が得られる。
米国特許第４，１３７，１４７号明細書は、蒸留点が約３６０℃より低く、１分子当たり少なくとも４個の炭素原子を有する直鎖パラフィン類およびイソパラフィン類を少なくとも含有する装荷物からエチレンおよびプロピレンを製造する方法に関する。該方法では、前記装荷物は、水素化分解区域内にて、触媒の存在下で水素化分解反応に付され、（ｂ）水素化分解反応からの流出物が、分離区域に送られ、（ｉ）該区域の頂部から、メタンおよび場合により水素が、（ｉｉ）該区域から１分子当たり２および３個の炭素原子を有する炭化水素から本質的になる留分が、（ｉｉｉ）該区域の底部から、１分子当たり少なくとも４個の炭素原子を有する炭化水素から本質的になる留分が排出され、（ｃ）前記１分子当たり２および３個の炭素原子を有する炭化水素から本質的になる留分のみ、蒸気の存在下で水蒸気分解区域に送られて、１分子当たり２および３個の炭素原子を有する炭化水素の少なくとも一部をモノオレフィン系炭化水素に転換し；前記分離区域の底部から得られた、前記１分子当たり少なくとも４個の炭素原子を有する炭化水素から本質的になる留分が、触媒の存在下でそれが処理される第２の水素化分解区域に送られ、第２の水素化分解区域からの廃液が、分離区域に送られて、一方では、１分子当たり少なくとも４個の炭素原子を有する炭化水素が排出され、その少なくとも一部が前記第２の水素化分解区域に再循環され、他方では、水素と、メタンと１分子当たり２および３個の炭素原子を有する飽和炭化水素との混合物から本質的になる留分が排出され；水素の流れおよびメタンの流れが前記混合物から分離され、２および３個の炭素原子を有する前記混合物の炭化水素が、第１の水素化分解区域に続く前記分離区域から回収された、１分子当たり２および３個の炭素原子を有する炭化水素から本質的になる前記留分と共に、前記水蒸気分解区域に送られる。このようにして、水蒸気分解区域の出口では、メタンおよび水素の流れと、１分子当たり２および３個の炭素原子を有するパラフィン系炭化水素の流れに加えて、１分子当たり２および３個の炭素原子を有するオレフィンと、１分子当たり少なくとも４個の炭素原子を有する生成物が得られる。
欧州特許出願公開第０２１９１９５号明細書は、炭化水素化合物からなる供給物を、水素の存在下で触媒上へ接触させて、縮合二環式ヒドロ芳香族炭化水素化合物を選択的に水素化し、かつ水蒸気分解して、分子量がより低く、より高いオクタン生成物を生成することによって、炭化水素化合物からなる前記供給物を沸点がより低く、オクタン価がより高い炭化水素に転換する方法に関する。
国際公開第２０１２／０７１１３７号公報は、ガスクラッカー供給原料を調製する方法に関する。該方法は、４〜１２個の炭素原子を有するパラフィン類の１種以上を含有する供給物を、水素の存在下で温度と圧力をそれぞれ上昇させて、触媒と接触させるステップと、供給物中の４〜１２個の炭素原子を有するパラフィン類の合計質量に対して、４〜１２個の炭素原子を有するパラフィン類の少なくとも４０ｗｔ％を、エタンおよび／またはプロパンに転換して、エタンおよび／またはプロパンを含む水蒸気分解したガスクラッカー供給原料を得るステップと、を備える。
米国特許第６，１８７，９８４号明細書は、ｎ−ブタンを含有する供給原料を、触媒の存在下でｎ−ブタンのブテン類への転換に適した反応条件下で接触させるステップを備える、ｎ−ブタンのブテン類への脱水素化方法に関する。
米国特許出願公開第２００３／２３２７２０号明細書は、脱水素可能な炭化水素を脱水素化複合触媒と接触させて、脱水素化した炭化水素を得るステップを含む、脱水素可能な炭化水素を脱水素化する方法に関する。 US Patent Application No. 2007/062848 is at least 20% by weight of one or more aromatics containing at least two fused aromatic rings, substituted or unsubstituted with up to two C1-4 alkyl groups. It relates to the step of hydrocracking a feed containing the compound to produce a product stream comprising at least 35% by weight of a C2-4 alkane mixture. In US Patent Application No. 2007/062848, bitumen from oil sands is fed to a conventional distillation apparatus, and the naphtha stream from the distillation apparatus is fed to a naphtha hydrotreating apparatus. The overhead gas stream is a light gas / light paraffin stream and is fed to the hydrocarbon cracker. The diesel stream from the distillation apparatus is supplied to a diesel hydrotreating apparatus, the diesel oil stream from the distillation apparatus is supplied to a vacuum distillation apparatus, and the vacuum diesel oil stream from the vacuum distillation apparatus is supplied to a diesel oil hydroprocessing apparatus. The light gas stream from the light oil hydrotreater is fed to the hydrocarbon cracker. The hydrotreated vacuum gas oil from the vacuum gas oil hydrotreating apparatus is supplied to the catalytic cracking apparatus. The bottom stream from the vacuum distillation unit is a vacuum (heavy) residue and is sent to a heavy oil pyrolysis unit that produces many streams such as a naphtha stream sent to the naphtha hydrotreater, and the diesel stream is diesel The hydrotreated diesel is generated by being sent to the hydrotreating device, and the light oil stream is supplied to the vacuum gas oil hydrotreating device to obtain the hydrotreated gas oil stream supplied to the catalytic cracking device.
U.S. Pat. No. 4,137,147 discloses ethylene and propylene from packages containing at least linear paraffins and isoparaffins having a distillation point below about 360 ° C. and having at least 4 carbon atoms per molecule. It relates to a method of manufacturing. In the method, the load is subjected to a hydrocracking reaction in the presence of a catalyst in a hydrocracking zone, (b) the effluent from the hydrocracking reaction is sent to a separation zone, a fraction consisting essentially of i) methane and optionally hydrogen from the top of the zone, and (ii) hydrocarbons having 2 and 3 carbon atoms per molecule from the zone, (iii) From the bottom, a fraction consisting essentially of hydrocarbons having at least 4 carbon atoms per molecule is discharged, and (c) consisting essentially of hydrocarbons having 2 and 3 carbon atoms per molecule Only the fraction is sent to the steam cracking zone in the presence of steam to convert at least a portion of the hydrocarbons having 2 and 3 carbon atoms per molecule to monoolefinic hydrocarbons; Obtained from the said 1 minute A fraction consisting essentially of hydrocarbons having at least 4 carbon atoms per unit is sent to a second hydrocracking zone where it is treated in the presence of a catalyst and from the second hydrocracking zone. Waste liquid is sent to the separation zone, on the one hand, hydrocarbons with at least 4 carbon atoms per molecule are discharged, at least part of which is recycled to the second hydrocracking zone, on the other hand A fraction consisting essentially of a mixture of hydrogen, methane and saturated hydrocarbons having 2 and 3 carbon atoms per molecule is discharged; a hydrogen stream and a methane stream are separated from said mixture, And hydrocarbons of the mixture having 3 carbon atoms are essentially recovered from hydrocarbons having 2 and 3 carbon atoms per molecule recovered from the separation zone following the first hydrocracking zone. Na Together with the fraction, it is sent to the steam cracking zone. In this way, at the outlet of the steam cracking zone, 2 and 3 carbons per molecule in addition to a stream of methane and hydrogen and a stream of paraffinic hydrocarbons having 2 and 3 carbon atoms per molecule An olefin having atoms and a product having at least 4 carbon atoms per molecule are obtained.
EP-A-0219195 selectively feeds a hydrocarbon compound onto a catalyst in the presence of hydrogen to selectively hydrogenate the fused bicyclic hydroaromatic hydrocarbon compound, and It relates to a process for converting the feed of hydrocarbon compounds into a hydrocarbon having a lower boiling point and a higher octane number by steam cracking to produce a lower octane product with a lower molecular weight.
WO 2012/071137 relates to a method for preparing a gas cracker feedstock. The method comprises contacting a feed containing one or more paraffins having 4 to 12 carbon atoms with a catalyst at elevated temperatures and pressures, respectively, in the presence of hydrogen; Of paraffins having 4 to 12 carbon atoms with respect to the total mass of paraffins having 4 to 12 carbon atoms, and converting ethane and / or propane to ethane and / or propane. Obtaining a steam cracked gas cracker feedstock containing propane.
US Pat. No. 6,187,984 comprises contacting a feed containing n-butane under reaction conditions suitable for the conversion of n-butane to butenes in the presence of a catalyst. The present invention relates to a method for dehydrogenating n-butane to butenes.
U.S. Patent Application Publication No. 2003/232720 includes dehydrating a dehydrogenable hydrocarbon comprising contacting the dehydrogenable hydrocarbon with a dehydrogenation composite catalyst to obtain a dehydrogenated hydrocarbon. It relates to the method of raw materialization.

Claims

(A) supplying a hydrocarbon feed to the ring-opening reaction zone;
(B) Separating the effluent from (a) into a gas stream containing light boiling hydrocarbons, a liquid stream containing naphtha boiling range hydrocarbons, and a liquid stream containing diesel boiling range hydrocarbons. Supplying step;
(C) supplying the liquid stream containing naphtha boiling range hydrocarbons to a hydrocracking device;
(D) separating the reaction product of the hydrocracker in step (c) into an overhead gas stream containing light boiling hydrocarbons and a bottom stream containing BTX (a mixture of benzene, toluene and xylene). ;
(E) a steam cracker, a propane dehydrogenator, a butane dehydrogenator, and an overhead gas stream from the hydrocracker in step (d) and the gas stream from the separator in step (b) A process for upgrading a refinery heavy hydrocarbon to a petrochemical product comprising: supplying to at least one device selected from the group of combined propane-butane dehydrogenation devices.

After separating the overhead gas stream from the hydrocracker in step (d) and the gas stream from the separator in step (b), and a hydrogen-containing stream from the gas stream, a steam cracker and propane dehydration 2. The process of claim 1, wherein the process is fed to at least one device selected from the group of elemental devices, butane dehydrogenators and propane-butane combined dehydrogenators.

Supplying the overhead gas stream from the hydrocracker in step (d) and the gas stream from the separator in step (b) to another separator; process according to claim 2 and providing the a cracker to dehydrogenation unit, and further comprising a.

The dehydrogenation process is a catalytic process, the process according to any one of claims 1 to 3, wherein the steam cracking process is a thermal cracking process.

In Fang aromatic compound extraction device, and further comprising the step of the hydrocarbon feed pretreatment, aromatics-rich stream is supplied to the ring-opening reaction zone from the aromatics extraction unit the process according to any one of claims 1 to 4.

The process of claim 5, wherein the aromatic compound extraction device is selected from the group of distillation device type, molecular sieve type and solvent extraction device type.

Pre-treating the hydrocarbon feedstock in a splitter apparatus in which a naphtha boiling range hydrocarbon fraction is fed directly into the hydrocracking unit and the heavy fraction is fed into the ring-opening reaction zone. The process according to claim 5 or 6, further comprising:

A heavy hydrocarbon fraction is fed to the ring-opening reaction zone, a stream containing naphtha boiling range hydrocarbons is fed directly to the hydrocracking unit, and a gas stream containing LPG is fed to a steam cracking unit and propane dehydrogenation. Pretreating said hydrocarbon feedstock in a prehydrocracking unit fed to one or more units selected from the group of a unit, a butane dehydrogenation unit and a combined propane-butane dehydrogenation unit The process according to claim 5, further comprising:

A BTXE type stream is obtained, a heavy hydrocarbon fraction is fed to the ring-opening reaction zone, and a gas stream containing LPG is combined with a steam cracker, a propane dehydrogenator, a butane dehydrogenator and a propane-butane combination. Pre-treating said hydrocarbon feedstock in a hydrodealkylation / reformation type device fed to one or more devices selected from the group of dehydrogenation devices A process according to any one of claims 5 to 8.

At least one of the gas stream from the separator of step (b), the gas stream from the hydrodealkylation / reformation type apparatus, and the gas stream from the prehydrocracking apparatus, the process according to any one of claims 1 to 9, further comprising the step of providing a reduction cracker.

The process according to any one of claims 3 to 10, further comprising the step of feeding the bottom stream from the hydrocracker to an alkyl exchange reactor.

The process according to any one of claims 1 to 11, further comprising the step of providing said liquid flow to aromatics saturation device comprising diesel boiling range hydrocarbons from the separator.

The overhead gas stream from the hydrocracker, the gas stream from the separator in step (b), and optionally the prehydrocracker and the hydrodealkylation / reforming type device. Separating the gas streams into individual streams each mainly comprising C2 paraffin, C3 paraffin and C4 paraffin, and supplying each individual stream to a specific furnace section of the steam cracker. The hydrogen-containing stream is sent to one or more hydrogen consuming process equipment;
Only C3-C4 fraction, the process according to any one of claims 1 to 12, further comprising the step of providing at least one pre-Symbol dehydrogenation unit.

14. The process of claim 13, wherein the hydrogen consuming process device is the (pre) hydrocracking device or the ring-opening reaction zone.

15. The process according to claim 13 or 14, further comprising the step of supplying only C3-C4 fractions as separate C3 and C4 streams to at least one of the dehydrogenators.

15. The process according to claim 13 or 14, further comprising the step of supplying only the C3-C4 fraction as a C3 + C4 mixed stream to at least one of the dehydrogenators.

As process conditions applied in the ring-opening reaction region, the temperature is 100 ° C. to 500 ° C., the pressure is 2 to 10 MPa, and the hydrogen amount per 1,000 kg of the raw material on the aromatic compound hydrogenation catalyst is 50 to 300 kg. And the obtained stream is sent to a ring cleavage apparatus having a temperature of 200 ° C. to 600 ° C., a pressure of 1 to 12 MPa, and a hydrogen amount of 50 to 200 kg per 1,000 kg of the obtained stream on the ring cleavage catalyst. The process according to any one of claims 1 to 16 .

The process according to any one of claims 1 to 17 , wherein the process conditions applied in the separation apparatus are a temperature of 149 ° C to 288 ° C and a pressure of MPa to 17.3 MPa. .

The process conditions applied in the hydrocracking apparatus include a reaction temperature of 300 to 580 ° C., a pressure of 0.3 to 5 MPa (gauge pressure ), and a mass space velocity (WHSV) per unit time of 0. the process according to any one of claims 1 to 18, characterized in that the .1~10 / h.

The process according to claim 19, characterized in that the reaction temperature is 450-580 ° C or 470-550 ° C.

The pressure is 0.6-3 MPa (gauge pressure), 1000-2000 kPa (gauge pressure), 1-2 MPa (gauge pressure), or 1.2-1.6 MPa (gauge) 21. Process according to claim 19 or 20, characterized in that

The mass space velocity (WHSV) per unit time is 0.2 to 6 / h, or 0.4 to 2 / h. process.

The process conditions applied in the steam cracker are a reaction temperature of 750 to 900 ° C., a residence time of 50 to 1000 ms, and a pressure selected from atmospheric pressure to 175 kPa (gauge pressure). The process according to any one of claims 1 to 22 .

The hydrocarbon feedstock in step (a) is shale oil, crude oil, kerosene, diesel, atmospheric pressure light oil (AGO), gas condensate, wax, crude oil mixed naphtha, reduced pressure gas oil (VGO), reduced pressure residue, atmospheric pressure residue. , Naphtha and pretreated naphtha, light circulating oil / heavy circulating oil (LCO / HCO), coke naphtha and diesel, FCC naphtha and diesel, slurry oil or combinations thereof 24. A process according to any one of claims 1 to 23 .

Use of diesel boiling range hydrocarbons as multistage ring-opening hydrocracked hydrocarbon feedstock as a raw material for aromatic compound saturators.

Use of a high-boiling range hydrocarbon fraction of a multistage ring-opening hydrocracked hydrocarbon raw material as a raw material for an alkyl exchange reactor.