JPS5820232A - Hydrocracking catalyst composition - Google Patents
Hydrocracking catalyst compositionInfo
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- JPS5820232A JPS5820232A JP11762181A JP11762181A JPS5820232A JP S5820232 A JPS5820232 A JP S5820232A JP 11762181 A JP11762181 A JP 11762181A JP 11762181 A JP11762181 A JP 11762181A JP S5820232 A JPS5820232 A JP S5820232A
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- alumina
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Abstract
Description
【発明の詳細な説明】
本発明は、水素化分解用触媒組成物に関し、詳しくは比
較的低温度に於いて重質油等の石油類を効率よく水素化
分解することのできる触媒組成物Ｋｌｌする〇
従来、アルギナやシリカアルミナなどの担体に活性金属
を担持させた水素化分解用触媒は知られている。しかし
これらの触媒を用いて重質油を水素化分解するには、高
温度において行なわなければならず、熱エネルギーを多
量に消費するという欠点があった。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a catalyst composition for hydrocracking, and more specifically to a catalyst composition Kll that can efficiently hydrocrack petroleum such as heavy oil at relatively low temperatures. 〇 Hydrocracking catalysts in which active metals are supported on carriers such as algina and silica alumina have been known. However, in order to hydrocrack heavy oil using these catalysts, the process must be carried out at high temperatures, which has the drawback of consuming a large amount of thermal energy.
本発明者らは上記従来技術の欠点を克服すべく鋭意研究
を重ね、轡に担体成分の開発に勢力を傾注した。その結
果、一般にアルコールの脱水素反応あるいは硫黄の吸着
剤外どとしてしか使用されていない酸化亜鉛を触媒担体
の一成分として用いると１重質油の水素分解を低温度に
て効率よく行表えることを見出した。本発明はかかる知
見に基いて完成したものである〇すなわち本発明は、酸
化亜鉛およびアルミナ系酸化物よりなる担体に、周期律
表第ＶＩＢ族に属する金属および第■族に属する金属よ
りなる活性金属を担持することを特徴とする水素化分解
用触媒組成物を提供するものである。The present inventors have conducted extensive research to overcome the drawbacks of the above-mentioned conventional techniques, and have concentrated their efforts on the development of carrier components. As a result, when zinc oxide, which is generally only used for alcohol dehydrogenation or as a sulfur adsorbent, is used as a component of the catalyst carrier, hydrogen decomposition of heavy oil can be carried out efficiently at low temperatures. I discovered that. The present invention has been completed based on this knowledge. In other words, the present invention provides a support made of zinc oxide and an alumina-based oxide, and an activated metal made of a metal belonging to group VIB of the periodic table and a metal belonging to group Ⅰ of the periodic table. The present invention provides a catalyst composition for hydrocracking characterized by supporting a metal.
本発明の触媒組成物は上述の如く担体と活性金属よシな
るものであるが、この担体は酸化亜鉛とアルミナ系酸化
物よシ構成されている。ここで担体を構成する酸化亜鉛
とアルミナ系酸化物の配合割合は特に制限はなく、各種
条件に応じて適宜選定すればよいが、通常は酸′化亜鉛
３〜６０重量哄およびアルミナ系酸化物９７〜４０重量
−１好ましくは酸化亜鉛５〜３０重量哄およびアルミナ
系酸化物９５〜７０重量％とすべきである。また、アル
ミナ系酸化物とは具体的には様々なものがあるが、例え
ばアルミナ、アルミナ−ゼオライト、アルミナ−ボリア
（ＡＪ、Ｏ。The catalyst composition of the present invention is composed of a carrier and an active metal as described above, and the carrier is composed of zinc oxide and an alumina-based oxide. There is no particular restriction on the blending ratio of zinc oxide and alumina-based oxide that constitute the carrier, and it may be selected appropriately depending on various conditions, but usually 3 to 60 kg of zinc oxide and alumina-based oxide are used. 97-40 wt-1 preferably 5-30 wt.% zinc oxide and 95-70 wt.% alumina based oxide. There are various alumina-based oxides, such as alumina, alumina-zeolite, and alumina-boria (AJ, O).
−Ｂ＊０ｓ）−アルミナ−ボリア−ゼオライト、アルミ
ナ−シリカ（にらＯ，−８ｉ０．）などをあげることが
で色る。-B*0s)-alumina-boria-zeolite, alumina-silica (Nira O, -8i0.), etc. can be cited.
一方、上記担体に担持させる活性金属は、周期律表第Ｖ
ＩＢ族に属する金属ならびに第■族に属する金属である
が、ここで第ＶＩＢ族に属する金属としてはクロム、モ
リブデン、タングステンがあるが、このうちモリブデン
およびタングステンを単独あるいは混合して用いること
が好ましい。On the other hand, the active metal supported on the carrier is listed in Periodic Table V.
Metals belonging to Group IB and metals belonging to Group Ⅰ, metals belonging to Group VIB include chromium, molybdenum, and tungsten, and among these, it is preferable to use molybdenum and tungsten alone or in combination. .
また、周期律表第■族に属する金属としては。Also, as a metal belonging to Group Ⅰ of the periodic table.
鉄、コバルト、ニッケル、ロジウム、パラジウム、白金
等各種のものがあるが、特にニッケル。There are various types of metal such as iron, cobalt, nickel, rhodium, palladium, and platinum, but nickel in particular.
コバルトが好ましく、これらを単独であるいは混合して
用いればよい。Cobalt is preferred, and these may be used alone or in combination.
上述の活性金属の担持量は、用いる担体、活性金属の種
類あるいは水素化分解すべき重質油の種類などに応じて
適宜定めればよいが、通常は担体１００重量部に対して
、第ＶＩＢ族に属する金属５〜２４重量部、好ましくは
７〜２０重量部および第■族に属する金属０．５〜８重
量部、好ましくは２〜７重量部の範囲とすべをである。The amount of the above-mentioned active metal supported may be determined as appropriate depending on the carrier used, the type of active metal, the type of heavy oil to be hydrocracked, etc., but it is usually 5 to 24 parts by weight, preferably 7 to 20 parts by weight of metals belonging to Group 1, and 0.5 to 8 parts by weight, preferably 2 to 7 parts by weight, of metals belonging to Group 1.
これらの活性金属を前述の担体に担持するにあたっては
、含浸、混練、共沈などの公知の方法によればよい。In order to support these active metals on the above-mentioned carrier, known methods such as impregnation, kneading, and coprecipitation may be used.
このようにして得られる触媒組成物を用いて効果的に水
素化分解することのできる原料油としては、原油の常圧
蒸留残渣油、減圧蒸留残渣油などの重質油である。もち
ろん、本発明の触媒組成物は、軽油９重質軽油、接触分
解残渣油。Feedstock oils that can be effectively hydrocracked using the catalyst composition obtained in this manner include heavy oils such as atmospheric distillation residue oil and vacuum distillation residue oil of crude oil. Of course, the catalyst composition of the present invention can be used for light oil, heavy gas oil, and catalytic cracking residue oil.
減圧軽油などの留出油の水素化分解にも適用しうるもの
である。It can also be applied to the hydrocracking of distillate oils such as vacuum gas oil.
また、本発明の触媒組成物を用いて水素化分解を実施す
る場合、従来から水素化分解に採用されている反応条件
を含む広範囲の反応条件を採用することができるが、従
来の反応温度よりもかなｐ低い温度で十分に水素化分解
が進行する。具体的な反応条件は、原料油の種類などに
より変動し、一義的に定めることはできないが、例えば
重質油の水素化分解の場合１通常は反応温度３４０−４
５０ｔｌ：、反応圧力８０〜２００ Ｙ−ｙ／ｅｘａ”
＊水素／原料油比３００〜２５００ Ｎｍ”／ＫＪ
、液時空間速度（ＬＨ８Ｖ ） ８．１〜Ｎ、Ｏｈｒ−
’とし、また水素は純度８０モ、ルチ以上のものが使用
されるｏ４Ｉに好ましい条“件としては、反応温度３８
０〜４３０Ｃ９反応圧力１００〜１５０Ｋｐ／（が、水
素／原料油比５０ Ｑ 〜２０ Ｇｏ Ｎｍ”／ＩＩＪ
、 ＬＨ８Ｖｏ、ｚ 〜Ｇ、７ ｈｒ−”であり、水
素は純度８５モルチ以上である〇本発明の触媒組成物に
よれば、重質な原料油を水素化分解するにあたっても比
較的低温度で高い分解活性を示すため、分解に際して必
要な熱エネルギーを大巾に節約することができる。Furthermore, when carrying out hydrocracking using the catalyst composition of the present invention, a wide range of reaction conditions can be employed, including reaction conditions conventionally employed in hydrocracking; Hydrogenolysis proceeds sufficiently at low temperatures. Specific reaction conditions vary depending on the type of feedstock oil and cannot be unambiguously determined, but for example, in the case of hydrocracking of heavy oil, the reaction temperature is usually 340-4.
50 tl:, reaction pressure 80-200 Y-y/exa”
*Hydrogen/raw oil ratio 300-2500 Nm”/KJ
, liquid hourly space velocity (LH8V) 8.1~N, Ohr-
In addition, the preferred conditions for o4I, in which hydrogen has a purity of 80 moles or more, is used at a reaction temperature of 38 moles or more.
0 to 430 C9 reaction pressure 100 to 150 Kp/(but hydrogen/raw oil ratio 50 Q to 20 Go Nm"/IIJ
, LH8Vo,z ~G, 7 hr-'', and the hydrogen has a purity of 85 molti or higher. According to the catalyst composition of the present invention, even when heavy feedstock oil is hydrocracked, it can be performed at a relatively low temperature. Since it exhibits high decomposition activity, the thermal energy required for decomposition can be greatly saved.
しかも、得られる水素化分解油は良質なものであり、軽
質油の得率が高い。Moreover, the obtained hydrocracked oil is of good quality, and the yield of light oil is high.
従って本発明の触媒組成物は、石油精製工業の分野に有
効に利用することができるものであるＯ
次に本発明を実施例によシさらに詳しく説明する。Therefore, the catalyst composition of the present invention can be effectively utilized in the field of petroleum refining industry.Next, the present invention will be explained in more detail with reference to Examples.
実施例１
アルミナとしてｓ、ｏｌ含有するアルミン酸ソーダ水溶
液＆、２９９に２１）の５０−グルコン酸水醇液を加え
て攪拌し、８，４チの硫酸アルミニラム水１１１１ｉｔ
ｐＨ９，ｓになるまで約８．３ Ｋ９を急速に加えた。Example 1 A sodium aluminate aqueous solution containing s and ol as alumina & 50-gluconic acid aqueous solution of 21) was added to 299 and stirred, and 1111 liters of 8.4 t aluminum sulfate water was prepared.
Approximately 8.3 K9 was added rapidly until the pH was 9.s.
次いで得られた混合物を一夜静置熟成後、ｆ別し、沈澱
物を０．２−アンモニア水で洗浄してアルミナヒドロゲ
ルを得た。The resulting mixture was then left to age overnight, separated, and the precipitate was washed with 0.2-ammonia water to obtain an alumina hydrogel.
一方、シリカ対アルミナのモル比が！Ｌ３２であるアン
モニウムイオン交換Ｙ型ゼオライトを、１気圧の水蒸気
雰囲気下で５４０ＣＫて焼成した。On the other hand, the molar ratio of silica to alumina! The ammonium ion-exchanged Y-type zeolite L32 was calcined at 540CK in a steam atmosphere of 1 atm.
なおこの際の水蒸気の流速は毎分７００ＣＣでありた。Note that the flow rate of water vapor at this time was 700 cc/min.
上記水蒸気処理後、ｌ規定の塩化アン毫ニウム溶液の過
剰量で室温にて２０時間処理してアンモニウム型とし、
次いで乾燥空気中で３時間焼成してＵＳ−Ｙ型ゼオツイ
トを得九。After the above steam treatment, it is treated with an excess amount of l-normal ammonium chloride solution at room temperature for 20 hours to form the ammonium form,
Then, it was calcined in dry air for 3 hours to obtain US-Y type zeotite.
続いて、上記アルミナヒドロゲルＩＫ２．上記ｕｓ −
ｙ ｍゼオライト２６４ｐ、硝酸亜鉛１５４？および水
ＩＪを加えて、ニーダ−で捏和し九後、直径０．９−の
ペレットに成形し、空気中１１０Ｃで１６時間乾燥後、
５５０Ｃア３時間焼成してＵＳ−Ｙ型ゼオライト含量４
０ｗｔ％、酸化亜鉛含１ｔ９Ｗｔｌアルミナ含量５１Ｗ
ｔ−の触媒担体を得た。Subsequently, the above alumina hydrogel IK2. Above us-
ym zeolite 264p, zinc nitrate 154? and water IJ were added, kneaded in a kneader, formed into pellets with a diameter of 0.9, and dried in air at 110C for 16 hours.
US-Y type zeolite content 4 after firing at 550C for 3 hours
0wt%, zinc oxide content 1t9Wtl alumina content 51W
A t-catalyst carrier was obtained.
さらに、との担体フＳｏ）にパラタングステン酸アンモ
ン２３３） 、硝酸ニッケル１３２？を含む水溶液４０
０ｍを加えて含浸させた後、 ２５０Ｃまで徐々に昇温
しながら乾燥した。次いで５５０Ｃで２時間焼成してタ
ングステン担持量およびニッケル担持量がそれぞれ金属
としてＩＬ５重量部および４．１重量部（担体１００重
量部に対して）である触媒組成物を製造した。In addition, ammonium paratungstate 233) and nickel nitrate 132? an aqueous solution containing 40
After adding 0m of water and impregnating it, it was dried while gradually raising the temperature to 250C. Then, the catalyst composition was calcined at 550 C for 2 hours to produce a catalyst composition having a supported amount of tungsten and a supported amount of nickel of IL of 5 parts by weight and 4.1 parts by weight (based on 100 parts by weight of the support), respectively.
実施例２
実施例１で得られたアルミナヒドロゲルＩＫ２゜実施例
１で得られたＵ８−ＹＷゼオライト６３５ｉ 。Example 2 Alumina hydrogel IK2° obtained in Example 1 U8-YW zeolite 635i obtained in Example 1.
硝酸亜鉛２０Ｓｆおよび水ＩＪを加えて、ニーダーで捏
和した後、直径０．９−のペレットに成形し、空気中１
１ＯＣで１６時間乾燥後、５５０Ｃで３時間焼成してＵ
Ｓ−Ｙ型ゼオライト含量ａｏｗｔチ、酸化亜鉛含量１２
ｗｔ％、アルミナ含量２８ｗｔ％の触媒担体を得た。After adding 20 Sf of zinc nitrate and IJ of water and kneading it with a kneader, it was formed into pellets with a diameter of 0.9 mm, and was heated in air for 1 hour.
After drying at 1OC for 16 hours, baking at 550C for 3 hours to obtain U.
S-Y type zeolite content aowt, zinc oxide content 12
A catalyst carrier having an alumina content of 28 wt% was obtained.
さらに、この担体７５０？にパラタングステン酸アンモ
ン２３３Ｆ 、硝酸ニッケル１３２）を含む水溶液４０
０−を加えて含浸させた後、２５０ｔ、ｔで徐々に昇温
しながら乾燥した。次いで５ｓｏＣで２時間焼成してタ
ングステン担持量およびニッケル担持量がそれぞれ金属
として１７．１重量部および４２重量部（担体１００重
量部に対して）である触媒組成物を製造した０
実施例３
実施例２で得られた担体６６０？に、硝酸コバルト１３
ｚｙ、パラモリブデン酸アンモン２９４ｆを含む水溶液
３９６１を加えて含浸させた後。Furthermore, this carrier 750? Aqueous solution 40 containing ammonium paratungstate 233F and nickel nitrate 132)
0- was added and impregnated, and then dried at 250 tons while gradually increasing the temperature. The catalyst composition was then calcined at 5soC for 2 hours to produce a catalyst composition having a supported amount of tungsten and a supported amount of nickel of 17.1 parts by weight and 42 parts by weight (based on 100 parts by weight of the support), respectively. Carrier 660 obtained in Example 2? , cobalt nitrate 13
zy, after adding and impregnating aqueous solution 3961 containing ammonium paramolybdate 294f.
２５０Ｃまで徐々に昇温しながら乾燥した。次いで５５
０Ｃで２時間焼成してコバルト担持量およびモリブデン
担持量がそれぞれ金属として３．９重量部および１６．
９重量部（担体１００重量部に対して）である触媒組成
物を製造した０
比較例１
実施例１で得られたアルミナとドロゲルｉｔｍ実施例１
で得られｐ Ｕ８−Ｙ型ゼオライ）２２９）および水Ｉ
Ｊを加えて、ニーダ−で捏和した後、直径０．９■のペ
レットに成形し、空気中１１０１：’で１６時間乾燥後
、５５０Ｃで３時間焼成、してＵＳ−Ｙ型ゼオライト含
１ｔ４０ＷｔＬ アルミナ含量（ｉＱＷｔ＄の触媒担
体を得喪。Drying was carried out while gradually raising the temperature to 250C. then 55
After firing at 0C for 2 hours, the amount of cobalt supported and the amount of molybdenum supported were 3.9 parts by weight and 16.9 parts by weight as metal, respectively.
Comparative Example 1 Alumina obtained in Example 1 and Drogel Itm Example 1
pU8-Y type zeolite) 229) and water I
J was added, kneaded in a kneader, formed into pellets with a diameter of 0.9 cm, dried in air at 1101:' for 16 hours, and then calcined at 550C for 3 hours to produce 1t40WtL containing US-Y type zeolite. Alumina content (iQWt$) catalyst support was obtained.
さらに、この担体７５０）にパラタングステン酸アンモ
ン２３３） 、硝酸ニッケル１３２）’ｉ含む水溶液４
００−を加えて含浸させた後、ｚｓｏｃまで徐々に昇温
しながら乾燥した。次いで５５０Ｃで２時間焼成してタ
ングステン担持゛量およびニッケル担持量がそれぞれ金
属として１７．０重量部および４．２５重量部（担体１
００重量部に対して）である触媒組成物を製造した０
比較例２
実施例１で得られたアルミナヒドロゲルＩ ＫＦ ＋実
施例１で得られたＵＳ−Ｙ型ゼオライ）２５１ｔ＊ホウ
酸９９ｆおよび水１１を加えて、ニーダーで捏和した後
、直径０．９−のペレットに成形し、空気中１ｌｏｔ：
’で１６時間乾燥後、５５０Ｃで３時間焼成してＵ８−
Ｙ Ｉｔゼオライト含量４９ｗｔ％。Furthermore, this carrier 750) contains an aqueous solution 4 containing ammonium paratungstate 233) and nickel nitrate 132)'i.
00- was added and impregnated, and then dried while gradually increasing the temperature to zsoc. Then, it was fired at 550C for 2 hours so that the amount of tungsten supported and the amount of nickel supported were 17.0 parts by weight and 4.25 parts by weight as metal, respectively (carrier 1
Comparative Example 2 Alumina hydrogel I KF obtained in Example 1 + US-Y type zeolite obtained in Example 1) 251t*boric acid 99f and After adding 11 parts of water and kneading with a kneader, it was formed into pellets with a diameter of 0.9 mm, and 1 lot was placed in air:
' After drying for 16 hours at 550C for 3 hours, U8-
Y It zeolite content 49wt%.
ボリア（ＢｍＯｓ）含量ｓｗｔチ、アルミナ含量５１ｗ
ｔ−の触媒担体を得た。Boria (BmOs) content swt, alumina content 51w
A t-catalyst carrier was obtained.
さらにここの担体ｙｓｏｔにパラタングステン酸アンセ
ン２３３ｆ、硝酸ニッケル１３２Ｆを含む水溶液４００
１を加えて含浸させた後、２５０Ｃまで徐々に昇温しな
がら乾燥した。次いで５ｓｏＣで２時間焼成してタング
ステン担持量およびニッケル担持量がそれぞれ金属とし
て１７．０重量部および４．２５重量部（担体１００重
量部に対して）である触媒組成物を製造した。Furthermore, an aqueous solution 400 containing paratungstate anthene 233F and nickel nitrate 132F is added to the carrier ysot.
1 was added and impregnated, and then dried while gradually raising the temperature to 250C. Subsequently, the catalyst composition was calcined at 5soC for 2 hours to produce a catalyst composition having a supported amount of tungsten and a supported amount of nickel of 17.0 parts by weight and 4.25 parts by weight (based on 100 parts by weight of the carrier), respectively.
比較例３ 実施例１で得られたアルミナヒドロゲルＩＫｙ。Comparative example 3 Alumina hydrogel IKy obtained in Example 1.
実施例１で得られｆｃＵ８−Ｙ型ゼオライト２９７ ｔ
ｅオルト珪酸ナトリウム２９５Ｐおよび水ＩＪを加え
て、ニーダーで捏和した後、直１ｊＯ，９ｓｍのペレッ
トに成形し、空気中１１００で１６時間乾燥後、５５０
Ｃで３時間焼成してＵＳ−Ｙ型ゼオライト含量４０ｗｔ
％、シリカ（８ｔ Ｏｘ ）含量９ ｗｔ ％ 。fcU8-Y type zeolite obtained in Example 1 297t
e Sodium orthosilicate 295P and water IJ were added and kneaded in a kneader, then directly formed into 1JO, 9sm pellets, dried in air at 1100C for 16 hours, and then heated at 550C.
Calcined for 3 hours at C, US-Y type zeolite content 40wt
%, silica (8tOx) content 9 wt%.
アルミ、す含量５１ｗｔ−の触媒担体を得た。A catalyst carrier having an aluminum content of 51 wt- was obtained.
さらに、この担体７５０？にパラタングステン酸アンモ
ン２３３Ｐ、硝酸ニッケル１３２？を含む水溶液４００
１を加えて含浸させた後、２５０Ｃまで徐々に昇温しな
がら乾燥した。次いで５ｓｏＣで２時間焼成してタング
ステン担持量およびニッケル担持量がそれぞれ金属とし
て１７．２重量部および４２重量部（担体１００重量部
に対して）である触媒組成物を製造した。Furthermore, this carrier 750? Ammonium paratungstate 233P, nickel nitrate 132? an aqueous solution containing 400
1 was added and impregnated, and then dried while gradually raising the temperature to 250C. Subsequently, the catalyst composition was calcined at 5soC for 2 hours to produce a catalyst composition having a supported amount of tungsten and a supported amount of nickel of 17.2 parts by weight and 42 parts by weight (based on 100 parts by weight of the carrier), respectively.
比較例４
実施例１て得られたアルミナヒドロゲル１ ’９ ｍ実
施例１で得られたＵＳ−Ｙｉｌゼオライ）Ｓ２７ｐおよ
び水１４を加えて、ニーダ−で捏和した後、直径０．９
■のベレットに成形し、空気中１１０ｃで１６時間乾燥
後、５５０ｃで３時間焼成してＵ８−Ｙ型ゼオライト含
量６０ｖｔ％、アルミナ含量４゜ｗｔ哄の触媒担体を得
た。Comparative Example 4 Alumina hydrogel obtained in Example 1 1'9m US-Yil zeolite obtained in Example 1) S27p and water 14 were added and kneaded in a kneader, and the diameter was 0.9 m.
The pellet was formed into a pellet (1), dried in air at 110°C for 16 hours, and then calcined at 550°C for 3 hours to obtain a catalyst carrier having a U8-Y type zeolite content of 60% by weight and an alumina content of 4°wt.
さらに、この担体７５６ＰＫパフタングステン酸アンモ
ン２３３ｆ、硝酸ニッケル１３２？を含む水＠１ｉ４０
０−を加えて含浸さセタ後、２５０Ｃまで徐々に昇温し
ながら乾燥した。次いで５５０ｃで２時間焼成してタン
グステン担持量およびニッケル担持量がそれぞれ金属と
して１７．３重量部および４．３重量部（担体１００重
量部に対して）である触媒組成物を製造し九。Furthermore, this carrier 756PK puffed ammonium tungstate 233f, nickel nitrate 132? Water containing @1i40
0- was added to impregnate the sample, and then the sample was dried while gradually increasing the temperature to 250C. Next, the catalyst composition was calcined at 550c for 2 hours to produce a catalyst composition having a supported amount of tungsten and a supported amount of nickel of 17.3 parts by weight and 4.3 parts by weight (based on 100 parts by weight of the carrier), respectively.9.
応用例１および参考例１〜３
原料油として大慶原油からの常圧蒸留残渣油を用い、反
応圧力（水素分圧）１３５にｙ／ｃａｒ” 、水素／油
比２００ＯＮｍｊハ（Ｊ 、 ＬＨ８Ｖ Ｏ，ｓ ｈｒ
−” Ｏ条件で反応温度を変化させ、また触媒として実
施例！および比較例１，２．’ｌで得られた組成物を用
いて、水素化分解反応を行なった。この水素化分解反応
による沸点３４３Ｃ以下の留分の得率（原料油に対する
重量％）ｔ−第１表に示す。Application example 1 and reference examples 1 to 3 Using atmospheric distillation residue oil from Daqing crude oil as the feedstock oil, the reaction pressure (hydrogen partial pressure) was 135 y/car, and the hydrogen/oil ratio was 200 ONmj (J, LH8V O, s hr
A hydrogenolysis reaction was carried out by changing the reaction temperature under O conditions and using the compositions obtained in Example! and Comparative Examples 1 and 2.1 as a catalyst. The yield of the fraction having a boiling point of 343C or less (% by weight relative to the raw material oil) is shown in Table 1.
応用例２，３および参考例４
原料油としてクラエート原油からの常圧蒸留残渣油を用
い、反応圧力（水素分圧） １３５ ＫＰ／ｃｄ 。Application Examples 2 and 3 and Reference Example 4 The atmospheric distillation residue oil from kraate crude oil was used as the raw material oil, and the reaction pressure (hydrogen partial pressure) was 135 KP/cd.
水素／油比２０００ Ｎｍ”／ ＫＪ 、 ＬＨ８Ｖ
Ｑ、 Ｂ ｈｒ−’ Ｏ条件で反応温度を変化させ、ま
た触媒として実施例２．３および比較例４で得られ九組
成物を用いて、水素化分解反応を行なった。この水素化
分解反応による沸点３４３Ｃ以下の留分の得率（原料油
に対する重量−）を第２表に示す０第２表
特許出願人 重質油対策技術研究組合Hydrogen/oil ratio 2000 Nm”/KJ, LH8V
A hydrogenolysis reaction was carried out by varying the reaction temperature under Q, B hr-' O conditions and using the nine compositions obtained in Example 2.3 and Comparative Example 4 as catalysts. Table 2 shows the yield of fractions with a boiling point of 343C or lower (weight relative to feedstock oil) through this hydrocracking reaction.0Table 2Patent Applicant: Heavy Oil Countermeasure Technology Research Association
Claims (4)
体に１周期律表第■Ｂ族に属する金属および第１族に属
する金属よりなる活性金属を担持することを特徴とする
水素化分解用触媒組成物。(1) A catalyst composition for hydrogenolysis, characterized in that an active metal consisting of a metal belonging to Group 1B of the periodic table and a metal belonging to Group 1 of the periodic table is supported on a carrier consisting of zinc oxide and alumina-based oxide. thing.
化物９７〜４０重量−よりなる担体１ＧＧ重量部に、周
期律表第ＶＨ２族に属する金属５〜２４重量部および第
１族に属する金属Ｏ，Ｓ〜８重量部を担持することを特
徴とする特許請求の範囲第１項記載の組成物。(2) 1 GG parts by weight of a carrier consisting of 3 to 60 parts by weight of zinc oxide and 97 to 40 parts by weight of an alumina-based oxide, and 5 to 24 parts by weight of a metal belonging to group VH2 of the periodic table and a metal O belonging to group 1 of the periodic table. , S to 8 parts by weight.
および／あるーはタングステンである特許請求の範囲第
１項記載の組成物。(3) The composition according to claim 1, wherein the metal belonging to BtjK of the periodic table is molybdenum and/or tungsten.
／あるいは＝パルトである特許請求の範囲第１項記載の
組成物。(4) The composition according to claim 1, wherein the metal belonging to Group I of the Periodic Table is nickel and/or Palt.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11762181A JPS5820232A (en) | 1981-07-29 | 1981-07-29 | Hydrocracking catalyst composition |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11762181A JPS5820232A (en) | 1981-07-29 | 1981-07-29 | Hydrocracking catalyst composition |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS5820232A true JPS5820232A (en) | 1983-02-05 |
Family
ID=14716279
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11762181A Pending JPS5820232A (en) | 1981-07-29 | 1981-07-29 | Hydrocracking catalyst composition |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5820232A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6013488A (en) * | 1983-07-05 | 1985-01-23 | Sony Corp | Digital phase servo circuit |
| JPS6013487A (en) * | 1983-07-05 | 1985-01-23 | Sony Corp | Digital speed servo circuit |
| JPS6015719A (en) * | 1983-07-07 | 1985-01-26 | Sony Corp | Digital phase servo circuit |
| JPS6361707A (en) * | 1986-09-01 | 1988-03-17 | Yoshie Nishizaki | Exhaust gas purifying and muffling device for internal combustion engine |
| JPH02299492A (en) * | 1988-09-24 | 1990-12-11 | Pfu Ltd | Rotational speed control system for motor |
| US5686374A (en) * | 1994-09-01 | 1997-11-11 | Japan Energy Corporation | Catalyst for hydroprocessing |
| JP2015523907A (en) * | 2012-06-01 | 2015-08-20 | 中国石油天然気股▲ふん▼有限公司 | Heavy oil high-efficiency catalytic conversion cracking catalyst and production method thereof |
| CN107930648A (en) * | 2017-11-24 | 2018-04-20 | 福州大学 | A kind of heavy oil floating bed hydrocracking catalyst and preparation method thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4838884A (en) * | 1971-09-22 | 1973-06-07 | ||
| JPS57207546A (en) * | 1981-06-13 | 1982-12-20 | Shokubai Kasei Kogyo Kk | Hydrocracking catalyst composition and its production |
-
1981
- 1981-07-29 JP JP11762181A patent/JPS5820232A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4838884A (en) * | 1971-09-22 | 1973-06-07 | ||
| JPS57207546A (en) * | 1981-06-13 | 1982-12-20 | Shokubai Kasei Kogyo Kk | Hydrocracking catalyst composition and its production |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6013488A (en) * | 1983-07-05 | 1985-01-23 | Sony Corp | Digital phase servo circuit |
| JPS6013487A (en) * | 1983-07-05 | 1985-01-23 | Sony Corp | Digital speed servo circuit |
| JPS6015719A (en) * | 1983-07-07 | 1985-01-26 | Sony Corp | Digital phase servo circuit |
| JPS6361707A (en) * | 1986-09-01 | 1988-03-17 | Yoshie Nishizaki | Exhaust gas purifying and muffling device for internal combustion engine |
| JPH0421049B2 (en) * | 1986-09-01 | 1992-04-08 | Yoshe Nishizaki | |
| JPH02299492A (en) * | 1988-09-24 | 1990-12-11 | Pfu Ltd | Rotational speed control system for motor |
| US5686374A (en) * | 1994-09-01 | 1997-11-11 | Japan Energy Corporation | Catalyst for hydroprocessing |
| JP2015523907A (en) * | 2012-06-01 | 2015-08-20 | 中国石油天然気股▲ふん▼有限公司 | Heavy oil high-efficiency catalytic conversion cracking catalyst and production method thereof |
| CN107930648A (en) * | 2017-11-24 | 2018-04-20 | 福州大学 | A kind of heavy oil floating bed hydrocracking catalyst and preparation method thereof |
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