JP3210729B2 - Method for reducing the amount of annular structures present in gas oil - Google Patents
Method for reducing the amount of annular structures present in gas oilInfo
- Publication number
- JP3210729B2 JP3210729B2 JP14110192A JP14110192A JP3210729B2 JP 3210729 B2 JP3210729 B2 JP 3210729B2 JP 14110192 A JP14110192 A JP 14110192A JP 14110192 A JP14110192 A JP 14110192A JP 3210729 B2 JP3210729 B2 JP 3210729B2
- Authority
- JP
- Japan
- Prior art keywords
- gas oil
- amount
- weight
- molar ratio
- zeolite
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
Landscapes
- Chemical & Material Sciences (AREA)
- Crystallography & Structural Chemistry (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)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、ガス油中に存在する環
状構造物の量を低減する方法に関する。This invention relates to a method for reducing the amount of annular structures present in gas oil.
【０００２】[0002]
【従来の技術】炭化水素油生成物は、それらば商業的に
適用されることになっているならば或る化学的及び物理
的要件を満たさねばならない、ということがよく知られ
ている。ガス油が満たさねばならない該要件のうちの一
つはセタン指数である。セタン指数に好ましく寄与する
化合物はパラフィンである。ナフテンのセタン指数への
寄与は好ましさが劣り、一方芳香族はその観点で好まし
さが更に劣る。所与のガス油のセタン指数を増大させる
ためにいくつかの方法が知られており、例えばハイドロ
クラッキング及び水素添加である。ハイドロクラッキン
グは、供給物の一部が不所望なより軽質の生成物に転化
されるという不利がある。水素添加は、オレフィン化合
物特に芳香族化合物を対応する飽和化合物に転化するこ
とからなる。分子の実質的なクラッキングを伴うことな
く所与のガス油に対して実行可能な最適セタン指数は、
かかるやり方では得られないであろう。更に、芳香族含
有量が少ないガス油を製造することが、環境上の観点か
ら重要である。BACKGROUND OF THE INVENTION It is well known that hydrocarbon oil products must meet certain chemical and physical requirements if they are to be applied commercially. One of the requirements that gas oil must meet is the cetane index. The compound that preferably contributes to the cetane index is paraffin. The contribution of naphthenes to the cetane index is less preferred, while aromatics are less preferred in that respect. Several methods are known for increasing the cetane index of a given gas oil, such as hydrocracking and hydrogenation. Hydrocracking has the disadvantage that a portion of the feed is converted to undesirable lighter products. Hydrogenation consists in converting olefinic compounds, especially aromatics, to the corresponding saturated compounds. The optimal cetane index feasible for a given gas oil without substantial cracking of the molecule is
It would not be obtained in such a manner. Furthermore, it is important from an environmental point of view to produce gas oils with low aromatic content.
【０００３】[0003]
【発明の解決点】ガス油中の環状構造物の量を低減する
特定の方法にガス油を付すことにより、良好なセタン指
数及び低芳香族含有率のガス油が商業的に魅力的な具合
で得られ得る、ということが今般見出された。かかる方
法で、存在する化合物のセタン指数が最適化される一
方、不所望なより軽質の生成物が生成する炭化水素のハ
イドロクラッキングは実質的に防止される。By subjecting the gas oil to a particular method of reducing the amount of cyclic structures in the gas oil, a gas oil of good cetane index and low aromatics content is a commercially attractive way. It has now been found that In such a way, the cetane index of the compounds present is optimized, while the hydrocracking of hydrocarbons, which leads to the formation of undesired lighter products, is substantially prevented.
【０００４】[0004]
【解決点の解決手段】本発明は、ガス油中に存在する環
状構造物の量を低減する方法において、２４．２０Ａと
２４．４０Ａとの間の単位格子サイズ並びに１０と１５
０との間のＳｉＯ2 ／Ａｌ2 Ｏ3 モル比を有する変性Ｙ
型ゼオライトからなる支持体に支持された１種又はそれ
以上の第VIII族貴金属からなる触媒を用いて、高められ
た温度と圧力にてガス油を水素と接触させ、そして低減
量の環状構造物を含むガス油を回収する、ことを特徴と
する上記方法に関する。The present invention is directed to a method for reducing the amount of annular structures present in gas oil, comprising a unit cell size between 24.20A and 24.40A and 10 and 15A.
Modified Y having a SiO 2 / Al 2 O 3 molar ratio between 0 and 0
Contacting gas oil with hydrogen at elevated temperature and pressure using a catalyst comprising one or more Group VIII noble metals supported on a support comprising type zeolite; And recovering gas oil containing the same.
【０００５】ガス油は、１７０℃と３９０℃との間の範
囲で沸とうする炭化水素を主として含みかつ２５０℃と
３９０℃との間の範囲で沸とうする炭化水素を少なくと
も２５重量％含有ししかも３８と４９との間のセタン指
数を有する炭化水素油を意味する。適当には、比較的軽
質のガス油即ち１７０℃と３２０℃との間の範囲で沸と
うする炭化水素を主として含むガス油が用いられる。好
ましくは水添処理されたガス油が用いられ、というのは
これらは比較的低い窒素及び硫黄の含有率を有してお
り、しかしてこれらの低い含有率は触媒の寿命に好まし
く寄与するからである。水添脱環化は、ガス油中に存在
する環状構造物の量の低減をなすと理解される。好まし
くは存在する環状構造物の量は、供給物中に存在する環
状構造物の量を基準として少なくとも１０％一層好まし
くは少なくとも１５％低減される。クラッキングは実質
的に起こらず、しかしてこのことは、本発明による方法
から回収されたガス油が供給物ガス油の９０重量％沸点
と供給物ガス油の最終沸点との間の範囲で沸とうする炭
化水素を少なくとも５重量％含むことを意味する。[0005] Gas oils contain predominantly hydrocarbons boiling in the range between 170 ° C and 390 ° C and contain at least 25% by weight of hydrocarbons boiling in the range between 250 ° C and 390 ° C. Moreover, it refers to a hydrocarbon oil having a cetane index between 38 and 49. Suitably, relatively light gas oils are used, i.e. gas oils mainly containing hydrocarbons boiling in the range between 170 ° C and 320 ° C. Preferably, hydrogenated gas oils are used, since they have a relatively low nitrogen and sulfur content, since these low contents favorably contribute to the life of the catalyst. is there. Hydrodecyclization is understood to result in a reduction in the amount of cyclic structures present in the gas oil. Preferably, the amount of cyclic structure present is reduced by at least 10%, more preferably at least 15%, based on the amount of cyclic structure present in the feed. Cracking does not occur substantially, which means that the gas oil recovered from the process according to the invention boils in the range between 90% by weight of the feed gas oil and the final boiling point of the feed gas oil. At least 5% by weight.
【０００６】本発明による方法において、１種又はそれ
以上の第VIII族貴金属を含む触媒が用いられる。適当に
存在し得る金属は、白金及び／又はパラジウムである。
好ましくは、該触媒は、ゼオライトの量を基準として
０．０５重量％と３重量％との間の貴金属を含む。一層
好ましくは、該触媒は０．２５と０．７５との間のモル
比の白金及びパラジウムを含む。該触媒は更に、１０と
１５０との間のＳｉＯ2 ／Ａｌ2 Ｏ3 モル比を有する変
性Ｙ型ゼオライトからなる支持体を含む。比較的低いＳ
ｉＯ2 ／Ａｌ2 Ｏ3 モル比の触媒が驚くべき程良好な結
果をもたらす、ということがわかった。好ましいモル比
は、１５と５０との間一層特に２０と４５との間にあ
る。適用されるＹ型ゼオライトの単位格子サイズは、２
４．２０Ａと２４．４０Ａとの間一層特に２４．２２Ａ
と２４．３５Ａとの間にある。水添脱環化は、適当には
１５０℃と４００℃との間の温度好ましくは２５０℃と
３８０℃との間の温度にて行われ得る。適用される水素
分圧は、通常１０バールと１５０バールとの間好ましく
は３０バールと１００バールとの間にあろう。In the process according to the invention, a catalyst containing one or more noble Group VIII metals is used. Suitable metals that may be present are platinum and / or palladium.
Preferably, the catalyst comprises between 0.05% and 3% by weight of noble metal, based on the amount of zeolite. More preferably, the catalyst comprises a molar ratio of platinum and palladium between 0.25 and 0.75. The catalyst further comprises a support comprising a modified Y-type zeolite having a SiO 2 / Al 2 O 3 molar ratio of between 10 and 150. Relatively low S
bring iO 2 / Al 2 O 3 molar ratio good results enough catalyst surprising, it was found that. Preferred molar ratios are between 15 and 50, more particularly between 20 and 45. The unit cell size of the applied Y-type zeolite is 2
Between 4.20A and 24.40A, more particularly 24.22A
And 24.35A. The hydrodecyclization may suitably be performed at a temperature between 150 and 400 ° C, preferably between 250 and 380 ° C. The hydrogen partial pressure applied will usually be between 10 and 150 bar, preferably between 30 and 100 bar.
【０００７】本方法において、触媒、温度及び圧力は一
般に、４５より大好ましくは５０より大のセタン指数を
有しかつ２５重量％未満好ましくは２０重量％未満の芳
香族化合物を含むガス油が生成されるような組合わせで
選ばれよう。５０より大のセタン指数を有しかつ５重量
％未満の芳香族化合物を含むガス油即ちいわゆる“生ガ
ス油”さえ、本方法において生成され得る、ということ
がわかった。セタン指数は、ＡＳＴＭ Ｄ９７６に従っ
て測定される。生成されるガス油の特性は、供給物ガス
油及びプロセス条件に左右される。商業的操作において
目ざされるセタン指数と芳香族含有率は、経済的な考慮
事情により決められる。In the present process, the catalyst, temperature and pressure generally produce a gas oil having a cetane index greater than 45, preferably greater than 50, and containing less than 25% by weight, preferably less than 20% by weight, of an aromatic compound. Let's choose the combination that will be done. It has been found that even gas oils having a cetane index of greater than 50 and containing less than 5% by weight of aromatics, ie so-called "raw gas oils", can be produced in the process. The cetane index is measured according to ASTM D976. The properties of the gas oil produced will depend on the feed gas oil and the process conditions. The intended cetane index and aromatics content in commercial operations are determined by economic considerations.
【０００８】[0008]
【実施例】本発明の方法を、次の例により更に説明す
る。 例 表１に記載の水添処理された直留ガス油を、２４．２４
Ａの単位格子サイズ及び４０のＳｉＯ2 ／Ａｌ2 Ｏ3 モ
ル比を有しかつゼオライトの量を基準として０．３重量
％の白金及び０．５重量％のパラジウムを含有するＹ型
ゼオライトからなる触媒と、２６５℃の温度、３５バー
ルの水素分圧及び１．４トン／ｍ3 ．ｈｒの重量時間空
間速度にて接触させた。得られた結果を表２に示す。得
られた生成物中に存在する環状構造物の量は、供給物中
に存在していた環状構造物の量を基準として１８％低減
された。The method of the present invention is further illustrated by the following example. Example The hydrogenated straight-run gas oil described in Table 1 was converted to 24.24.
Consisting of a unit cell size of A and a SiO 2 / Al 2 O 3 molar ratio of 40 and comprising a Y-type zeolite containing 0.3% by weight of platinum and 0.5% by weight of palladium, based on the amount of zeolite. The catalyst, a temperature of 265 ° C., a hydrogen partial pressure of 35 bar and 1.4 ton / m 3 . The contact was made at a weight hourly space velocity of hr. Table 2 shows the obtained results. The amount of cyclic structure present in the resulting product was reduced by 18% based on the amount of cyclic structure present in the feed.
【０００９】[0009]
【表１】表 １ 沸点分布（℃） 初期沸点 １７９ １０％ ２０５ ３０％ ２１８ ５０％ ２３３ ７０％ ２４９ ９０％ ２７２ 最終沸点 ２９４ セタン指数 ４９．３ 芳香族含有率（容量％） ２０．１Table 1 Table 1 Boiling point distribution (° C) Initial boiling point 179 10% 205 30% 218 50% 233 70% 249 90% 272 Final boiling point 294 Cetane index 49.3 Aromatic content (% by volume) 20.1
【００１０】[0010]
【表２】表 ２ 沸点分布（℃） 初期沸点 １８０ １０％ ２０５ ３０％ ２１８ ５０％ ２３１ ７０％ ２４７ ９０％ ２７２ 最終沸点 ２９３ セタン指数 ５３．４ 芳香族含有率（容量％） ３．９ Table 2 Boiling point distribution (° C.) Initial boiling point 180 10% 205 30% 218 50% 231 70% 247 90% 272 Final boiling point 293 Cetane index 53.4 Aromatic content (% by volume) 3.9
───────────────────────────────────────────────────── フロントページの続き (72)発明者 ジヤツク・ルシエン オランダ国 2596 エイチ・アール、ハ ーグ、カレル・ウアン・ビラントラーン 30 (72)発明者 ゲラルダス・レオナルダス・ボスコ・ス イーエレマンス オランダ国 2596 エイチ・アール、ハ ーグ、カレル・ウアン・ビラントラーン 30 (56)参考文献 特開 昭62−294443（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) C10G 49/08 B01J 29/12 C10G 47/18 ──────────────────────────────────────────────────続 き Continued on the front page (72) Inventor Jacques Lucien, Netherlands 2596 H.R.H.H., Karel Wan-Bilantran 30 (72) Inventor Geraldas Leonardas Bosco S.E.E.M.Netherlands 2596 H.E. Earl, Hague, Karel Wan-Billantran 30 (56) References JP-A-62-294443 (JP, A) (58) Fields investigated (Int. Cl. 7 , DB name) C10G 49/08 B01J 29 / 12 C10G 47/18
Claims (9)
減する方法において、２４．２０Ａと２４．４０Ａとの
間の単位格子サイズ並びに１０と１５０との間のＳｉＯ
2 ／Ａｌ2 Ｏ3 モル比を有する変性Ｙ型ゼオライトから
なる支持体に支持された１種又はそれ以上の第ＶＩＩＩ
族貴金属からなる触媒を用いて、高められた温度と圧力
にてガス油を水素と接触させ、そして低減量の環状構造
物と、供給物ガス油の９０重量％沸点と供給物ガス油の
最終沸点との間の範囲で沸とうする炭化水素を少なくと
も５重量％含むガス油を回収する、そして前記触媒は本
質的にいかなる非晶質熱分解成分も含まないことを特徴
とする上記方法。1. A method for reducing the amount of cyclic structures present in a gas oil, comprising a unit cell size between 24.20 A and 24.40 A and a SiO 2 between 10 and 150.
One or more VIIIs supported on a support comprising a modified Y zeolite having a 2 / Al 2 O 3 molar ratio
The gas oil is contacted with hydrogen at elevated temperature and pressure using a catalyst consisting of group noble metals and a reduced amount of annular structure , 90% by weight of the feed gas oil boiling point and the feed gas oil
Reduce the amount of hydrocarbons boiling between the final boiling point
Recovering a gas oil which also contains 5% by weight , and wherein the catalyst is essentially free of any amorphous pyrolysis components.
のＳｉＯ2 ／Ａｌ2Ｏ3 モル比を有する、請求項１の方
法。2. The method of claim 1, wherein the modified Y zeolite has a SiO 2 / Al 2 O 3 molar ratio between 15 and 50.
のＳｉＯ2 ／Ａｌ2Ｏ3 モル比を有する、請求項２の方
法。3. The method of claim 2, wherein the modified Y zeolite has a SiO 2 / Al 2 O 3 molar ratio between 20 and 45.
４．３５Ａとの間の単位格子サイズを有する、請求項１
〜３のいずれか一つの項の方法。4. The modified Y zeolite has 24.22 A and 2
2. A unit cell size having a unit cell size of between 4.35A.
3. The method according to any one of items 1 to 3.
う、請求項１〜４のいずれか一つの項の方法。5. The method according to claim 1, which is carried out at a temperature between 150 ° C. and 400 ° C.
分圧にて行う、請求項１〜５のいずれか一つの項の方
法。6. The process as claimed in claim 1, wherein the process is carried out at a partial pressure of hydrogen of between 10 and 150 bar.
比の白金及びパラジウムを含む、請求項１〜６のいずれ
か一つの項の方法。7. The process according to claim 1, wherein the catalyst comprises platinum and palladium in a molar ratio between 0.25 and 0.75.
つ５０より大のセタン指数を有するガス油を回収する、
請求項１〜７のいずれか一つの項の方法。8. recovering a gas oil containing less than 25% by weight aromatics and having a cetane index greater than 50;
A method according to any one of claims 1 to 7.
５０より大のセタン指数を有するガス油を回収する、請
求項１〜８のいずれか一つの項の方法。9. The process according to claim 1, wherein a gas oil containing less than 5% by weight of aromatic compounds and having a cetane index greater than 50 is recovered.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB919110012A GB9110012D0 (en) | 1991-05-09 | 1991-05-09 | Hydrodecyclization process |
| GB9110012.3 | 1991-05-09 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH05179260A JPH05179260A (en) | 1993-07-20 |
| JP3210729B2 true JP3210729B2 (en) | 2001-09-17 |
Family
ID=10694685
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP14110192A Expired - Fee Related JP3210729B2 (en) | 1991-05-09 | 1992-05-07 | Method for reducing the amount of annular structures present in gas oil |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0512652B1 (en) |
| JP (1) | JP3210729B2 (en) |
| CA (1) | CA2068174C (en) |
| DE (1) | DE69204206T2 (en) |
| DK (1) | DK0512652T3 (en) |
| ES (1) | ES2077338T3 (en) |
| FI (1) | FI114317B (en) |
| GB (1) | GB9110012D0 (en) |
| NO (1) | NO304029B1 (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FI102767B (en) | 1997-05-29 | 1999-02-15 | Fortum Oil Oy | Process for the production of high quality diesel fuel |
| US6444865B1 (en) | 1997-12-01 | 2002-09-03 | Shell Oil Company | Process wherein a hydrocarbon feedstock is contacted with a catalyst |
| KR100438816B1 (en) * | 1998-03-09 | 2004-07-16 | 삼성전자주식회사 | Personal solid image head mount display device, especially including two dimensional image display |
| DE19949211A1 (en) * | 1999-10-13 | 2001-05-31 | Veba Oel Ag | Process for the preparation of n-alkanes from mineral oil fractions and catalyst for carrying out the process |
| KR100419288B1 (en) * | 2001-06-22 | 2004-02-19 | 인천정유 주식회사 | Method for preparing catalysts for dearomatization in distillate |
| ES2200702B1 (en) * | 2002-07-16 | 2005-05-01 | Univesidad Politecnica De Valencia | CATALYST CONTAINING A MICROPOROUS CRYSTAL SOLID MATERIAL AND PROCESS TO IMPROVE THE QUALITY OF DIESEL FRACTIONS USING SUCH CATALYST. |
| CN105713657B (en) * | 2014-12-01 | 2017-05-17 | 中国石油化工股份有限公司 | Hydrocracking method |
| US11001765B2 (en) | 2016-02-25 | 2021-05-11 | Sabic Global Technologies B.V. | Process for combined hydrodesulfurization and hydrocracking of heavy hydrocarbons |
| CN108699449A (en) * | 2016-03-01 | 2018-10-23 | 沙特基础工业全球技术有限公司 | Method for producing mononuclear aromatics by the hydrocarbon charging comprising polycyclic aromatic hydrocarbon |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8613131D0 (en) * | 1986-05-30 | 1986-07-02 | Shell Int Research | Hydrocarbon conversion |
-
1991
- 1991-05-09 GB GB919110012A patent/GB9110012D0/en active Pending
-
1992
- 1992-05-07 NO NO921806A patent/NO304029B1/en unknown
- 1992-05-07 FI FI922069A patent/FI114317B/en active IP Right Grant
- 1992-05-07 DE DE69204206T patent/DE69204206T2/en not_active Expired - Fee Related
- 1992-05-07 CA CA002068174A patent/CA2068174C/en not_active Expired - Fee Related
- 1992-05-07 ES ES92201302T patent/ES2077338T3/en not_active Expired - Lifetime
- 1992-05-07 EP EP92201302A patent/EP0512652B1/en not_active Expired - Lifetime
- 1992-05-07 DK DK92201302.4T patent/DK0512652T3/en active
- 1992-05-07 JP JP14110192A patent/JP3210729B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| EP0512652B1 (en) | 1995-08-23 |
| CA2068174C (en) | 2003-12-02 |
| FI114317B (en) | 2004-09-30 |
| NO304029B1 (en) | 1998-10-12 |
| ES2077338T3 (en) | 1995-11-16 |
| NO921806D0 (en) | 1992-05-07 |
| DE69204206T2 (en) | 1996-02-01 |
| FI922069A0 (en) | 1992-05-07 |
| NO921806L (en) | 1992-11-10 |
| FI922069A (en) | 1992-11-10 |
| EP0512652A1 (en) | 1992-11-11 |
| GB9110012D0 (en) | 1991-07-03 |
| DK0512652T3 (en) | 1995-09-25 |
| DE69204206D1 (en) | 1995-09-28 |
| JPH05179260A (en) | 1993-07-20 |
| CA2068174A1 (en) | 1992-11-10 |
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