JPH04122789A - Catalytic hydrocracking of heavy oil - Google Patents
Catalytic hydrocracking of heavy oilInfo
- Publication number
- JPH04122789A JPH04122789A JP24418390A JP24418390A JPH04122789A JP H04122789 A JPH04122789 A JP H04122789A JP 24418390 A JP24418390 A JP 24418390A JP 24418390 A JP24418390 A JP 24418390A JP H04122789 A JPH04122789 A JP H04122789A
- Authority
- JP
- Japan
- Prior art keywords
- heavy oil
- reactor
- catalyst
- metal
- filled
- 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.)
- Pending
Links
- 239000000295 fuel oil Substances 0.000 title claims abstract description 17
- 238000004517 catalytic hydrocracking Methods 0.000 title claims abstract description 14
- 239000003054 catalyst Substances 0.000 claims abstract description 28
- 238000006243 chemical reaction Methods 0.000 claims abstract description 26
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 14
- 229910052751 metal Inorganic materials 0.000 claims abstract description 14
- 239000002184 metal Substances 0.000 claims abstract description 14
- 239000010457 zeolite Substances 0.000 claims abstract description 14
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 claims abstract description 12
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 5
- 239000001257 hydrogen Substances 0.000 claims abstract description 5
- 238000005342 ion exchange Methods 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 3
- -1 ammonium ions Chemical group 0.000 abstract description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 4
- 230000003197 catalytic effect Effects 0.000 abstract description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052681 coesite Inorganic materials 0.000 abstract description 2
- 229910052593 corundum Inorganic materials 0.000 abstract description 2
- 229910052906 cristobalite Inorganic materials 0.000 abstract description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract description 2
- 229910052750 molybdenum Inorganic materials 0.000 abstract description 2
- 229910052759 nickel Inorganic materials 0.000 abstract description 2
- 239000000377 silicon dioxide Substances 0.000 abstract description 2
- 235000012239 silicon dioxide Nutrition 0.000 abstract description 2
- 229910052682 stishovite Inorganic materials 0.000 abstract description 2
- 229910052905 tridymite Inorganic materials 0.000 abstract description 2
- 229910052721 tungsten Inorganic materials 0.000 abstract description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 abstract description 2
- 239000003921 oil Substances 0.000 abstract 2
- 238000007039 two-step reaction Methods 0.000 abstract 2
- YNPNZTXNASCQKK-UHFFFAOYSA-N phenanthrene Chemical compound C1=CC=C2C3=CC=CC=C3C=CC2=C1 YNPNZTXNASCQKK-UHFFFAOYSA-N 0.000 description 12
- 239000002994 raw material Substances 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 230000035484 reaction time Effects 0.000 description 5
- 238000004523 catalytic cracking Methods 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 239000011280 coal tar Substances 0.000 description 3
- 125000002950 monocyclic group Chemical group 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000007327 hydrogenolysis reaction Methods 0.000 description 2
- BBEAQIROQSPTKN-UHFFFAOYSA-N pyrene Chemical compound C1=CC=C2C=CC3=CC=CC4=CC=C1C2=C43 BBEAQIROQSPTKN-UHFFFAOYSA-N 0.000 description 2
- 238000007873 sieving Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000011269 tar Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 229910052684 Cerium Inorganic materials 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 150000001242 acetic acid derivatives Chemical class 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 210000000988 bone and bone Anatomy 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- HHNHBFLGXIUXCM-GFCCVEGCSA-N cyclohexylbenzene Chemical compound [CH]1CCCC[C@@H]1C1=CC=CC=C1 HHNHBFLGXIUXCM-GFCCVEGCSA-N 0.000 description 1
- 125000005832 cyclohexylphenylene group Chemical group [H]C1=C([H])C(=C([H])C([H])=C1[*:2])C1([H])C([H])([H])C([H])([H])C([H])([*:1])C([H])([H])C1([H])[H] 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- GVEPBJHOBDJJJI-UHFFFAOYSA-N fluoranthrene Natural products C1=CC(C2=CC=CC=C22)=C3C2=CC=CC3=C1 GVEPBJHOBDJJJI-UHFFFAOYSA-N 0.000 description 1
- 238000002290 gas chromatography-mass spectrometry Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 229910052740 iodine Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 239000003027 oil sand Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 235000021317 phosphate Nutrition 0.000 description 1
- 150000003013 phosphoric acid derivatives Chemical class 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 1
Landscapes
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
【発明の詳細な説明】
産業上の利用分野
本発明は、多環芳香族炭化水素類を含有する重質油の接
触分解方法に関する。DETAILED DESCRIPTION OF THE INVENTION Field of the Invention The present invention relates to a method for catalytic cracking of heavy oil containing polycyclic aromatic hydrocarbons.
以下、本明細書中に「％」とあるのは１重量％」を意味
する。Hereinafter, "%" in this specification means "1% by weight".
従来の技術とその問題点
一般にコールタールは、ベンセン、ナフタレン、アルキ
ルナフタレン、フェナントレン、アントラセノ、ピレン
などの芳香族炭化水素類を含有している。BACKGROUND OF THE INVENTION Coal tar generally contains aromatic hydrocarbons such as benzene, naphthalene, alkylnaphthalene, phenanthrene, anthraceno, and pyrene.
特に、ベンセンおよびナフタレンは、あらゆる化成品の
基幹原料として利用されており、一方アルキルナフタレ
ンは、近年注目されている耐熱性かつ高強度の樹脂原料
として利用されつつある。In particular, benzene and naphthalene are used as basic raw materials for all kinds of chemical products, while alkylnaphthalenes are being used as heat-resistant and high-strength resin raw materials that have been attracting attention in recent years.
しかしながら、コールタール中に多量に含まれている３
環以上の多環芳香族炭化水素類については、まだ化学原
料として有効に利用されるまでに至っていないのが現状
である。例えば、フエナントレンは、ナフタレンについ
て含量が多く （５％程度）、その生産量は日本だけで
も年間１３万トンにも達しているのにもかかわらず、接
触転化か困難な物質であるため主にカーボンブラックの
製造原料として用いられているに過ぎない。However, coal tar contains a large amount of 3
At present, polycyclic aromatic hydrocarbons having more than a ring have not yet been effectively utilized as chemical raw materials. For example, phenanthrene has a high content of naphthalene (approximately 5%), and its production amount reaches 130,000 tons per year in Japan alone. It is only used as a raw material for producing black.
したがって、現在のところ利用価値が低いとされている
上記多環芳香族炭化水素類を単環あるいは２環芳香族炭
化水素に効率よく転換しうる新たな技術の開発が切望さ
れている。Therefore, there is a strong need for the development of a new technology that can efficiently convert the polycyclic aromatic hydrocarbons, which are currently considered to have low utility value, into monocyclic or bicyclic aromatic hydrocarbons.
問題点を解決するための手段
本発明者は、上記の接触転化における問題点に鑑み鋭意
研究を重ねた結果、２段接触水素化分解プロセスによっ
て、重質油を効率よく軽質化する方法を見出した。Means for Solving the Problems In view of the above problems in catalytic conversion, the present inventor has conducted extensive research and has discovered a method for efficiently lightening heavy oil by a two-stage catalytic hydrocracking process. Ta.
即ち、本発明は、下記の重質油の接触分解方法を提供す
るものである。That is, the present invention provides the following method for catalytic cracking of heavy oil.
■ 水素雰囲気下で２段反応により、多環芳香族炭化水
素類を含有する重質油を接触分解して軽質化するに際し
、上記２段反応の各反応器内に互いに触媒性能の異なる
触媒を充填し、反応条件をそれぞれ独立に制御すること
を特徴とする重質油の接触水素化分解方法６
■ 適当な酸性度をもつ水素化分解用金属担持触媒を第
１段反応の反応器内に充填する上記第１項記載の重質油
の接触水素化分解方法。■ When heavy oil containing polycyclic aromatic hydrocarbons is catalytically cracked and lightened by a two-stage reaction in a hydrogen atmosphere, catalysts with different catalytic performance are placed in each reactor of the two-stage reaction. A method for catalytic hydrocracking of heavy oil, characterized by charging and controlling the reaction conditions independently 6 ■ A supported metal catalyst for hydrocracking with appropriate acidity is placed in the reactor for the first stage reaction. The method for catalytic hydrocracking of heavy oil according to the above item 1, which is filled.
■ アンモニウムイオン置換型Ｙ−ゼオライトをイオン
交換に供することにより得られる金属担持ゼオライトを
第２段反応の反応器内に充填する上記第１項記載の重質
油の接触水素化分解方法。(2) The catalytic hydrocracking method for heavy oil according to the above item (1), wherein the metal-supported zeolite obtained by subjecting ammonium ion-substituted Y-zeolite to ion exchange is charged into the reactor for the second stage reaction.
以下、本発明方法について詳細に説明する。The method of the present invention will be explained in detail below.
本発明においては、まず第１段反応器内即ち適当な酸性
度を有する金属担持水素化分解触媒上で、第２段反応器
内に充填されているゼオライト系触媒の気孔に侵入でき
る大きさになるように多環芳香族炭化水素類を部分水素
化分解することにより骨核を小さくする。ついて得られ
た材料を第２段反応器内に導入し、金属担持ゼオライト
系触媒の分子ふるい作用によって化合物の種類が揃い、
単環および２環芳香族炭化水素が得られる。In the present invention, first, in the first stage reactor, that is, on the metal-supported hydrogenolysis catalyst with appropriate acidity, the catalyst is heated to a size that can penetrate into the pores of the zeolite catalyst packed in the second stage reactor. The bone core is made smaller by partially hydrogenolyzing polycyclic aromatic hydrocarbons. The resulting material is introduced into the second stage reactor, and the types of compounds are uniformed by the molecular sieving action of the metal-supported zeolite catalyst.
Monocyclic and bicyclic aromatic hydrocarbons are obtained.
本発明か処理の対象とする原料は、多環芳香族炭化水素
類そのものあるいは多環芳香族炭化水素を含有する重質
油（以下、特に必要でない限り、単に多環芳香族炭化水
素という）などである。The raw materials to be treated in the present invention include polycyclic aromatic hydrocarbons themselves, heavy oil containing polycyclic aromatic hydrocarbons (hereinafter simply referred to as polycyclic aromatic hydrocarbons unless otherwise required), etc. It is.
上記原料は、コールタール、オイルサンド系タール、石
油系重質油、バイオマス系タールなどから公知の技術に
より容易に製造することができる。The above raw materials can be easily produced from coal tar, oil sand tar, petroleum heavy oil, biomass tar, etc. using known techniques.
つぎに、本発明で用いる触媒として第１段反応器内には
適当な酸性度をもつ水素化分解用金属担持触媒を充填す
る。Next, as a catalyst used in the present invention, a supported metal catalyst for hydrogenolysis having an appropriate acidity is filled in the first stage reactor.
上記触媒の担体としては、Ａｌ２Ｏ３、Ｓ ｉＯ２、Ａ
１２０３ Ｓ Ｉ Ｏ２、カーボンブラックなどが
挙げられる。As the carrier for the above catalyst, Al2O3, SiO2, A
1203 S I O2, carbon black, and the like.
触媒活性成分としては、Ｃｏ、Ｍｏ、Ｎｉ、Ｗ、Ｉ ｒ
ＳＰｄ、Ｐｔ、ＲｈＳＲｕＳＡｇ５Ｃｕ。Catalyst active components include Co, Mo, Ni, W, I r
SPd, Pt, RhSRuSAg5Cu.
Ｎａ、におよびこれら金属の任意の組み合わせか使用さ
れる。これらの中でも特に、Ｃｏ５Ｍｏ。Na, and any combination of these metals may be used. Among these, especially Co5Mo.
Ｎ１５Ｗおよびこれらの組み合わせが好ましい。N15W and combinations thereof are preferred.
触媒金属の担持量は、酸化物として０，５〜３０％程度
とする。The amount of catalyst metal supported is approximately 0.5 to 30% as an oxide.
一方、第２段反応の反応器内にはアンモニウムイオン置
換型Ｙ−ゼオライトをイオン交換に供することにより調
製された、分子ふるい作用を有する金属担持ゼオライト
を充填する。On the other hand, the reactor for the second stage reaction is filled with metal-supported zeolite having a molecular sieving action, which is prepared by subjecting ammonium ion-substituted Y-zeolite to ion exchange.
ゼオライトに担持させる触媒活性成分としての金属は、
Ｎｉ、ＦｅＳＭｏ５Ｌａ、Ｃｏ、Ｒｈ。The metal as a catalytically active component supported on zeolite is
Ni, FeSMo5La, Co, Rh.
Ｐｔ、Ｚｎ５ＲｕＳＰｄＳＴｉ、Ｃｅ、Ｃｕなどが例示
できる。これらの中でも２環および単環芳香族炭化水素
への転換に優れた効果を示すＮｉが特に好ましい。Examples include Pt, Zn5RuSPdSTi, Ce, and Cu. Among these, Ni is particularly preferred since it exhibits excellent conversion effects into two-ring and mono-ring aromatic hydrocarbons.
ゼオライトに対する金属担持量は、金属の種類などによ
り異なるが、通常はゼオライト重量の０．５〜１０％程
度とする。また、金属源とじて使用する水溶性金属塩と
しては、硝酸塩、硫酸塩、酢酸塩、リン酸塩、炭酸塩、
塩化物などが例示できる。The amount of metal supported on the zeolite varies depending on the type of metal, etc., but is usually about 0.5 to 10% of the weight of the zeolite. Water-soluble metal salts used as metal sources include nitrates, sulfates, acetates, phosphates, carbonates,
Examples include chlorides.
接触分解による軽質化の反応条件としては、通常水素ガ
ス雰囲気中、上記触媒をそれぞれ各反応器に充填した後
、第１反応器内は３００〜７００°Ｃ程度、圧力３０〜
１２０ｋｇ／ＣｒＩ程度、反応時間１０分〜５時間程度
、第２段反応温度は３００〜５５０℃程度、圧力３０〜
１２０ｋｇ／ｃ−程度、反応時間１０分〜５時間程度で
ある。The reaction conditions for lightening by catalytic cracking are usually in a hydrogen gas atmosphere, after each reactor is filled with the above catalysts, the inside of the first reactor is about 300-700°C, and the pressure is 30-30°C.
Approximately 120 kg/CrI, reaction time approximately 10 minutes to 5 hours, second stage reaction temperature approximately 300 to 550°C, pressure 30 to
The weight is about 120 kg/c-, and the reaction time is about 10 minutes to 5 hours.
発明の効果
本発明によれば、従来までは充分に利用されていなかっ
た３環以上の多環芳香族炭化水素類から多様な用途をも
つ単環あるいは２環芳香族炭化水素を高転化率で得られ
るので、天然資源を有効に活用することができ、省エネ
ルギー化、製品の低コスト化などに非常に有利である。Effects of the Invention According to the present invention, it is possible to convert polycyclic aromatic hydrocarbons having three or more rings, which have not been sufficiently utilized in the past, to monocyclic or bicyclic aromatic hydrocarbons, which have a variety of uses, at a high conversion rate. As a result, natural resources can be used effectively, which is extremely advantageous in terms of energy conservation and product cost reduction.
実施例
以下、実施例および比較例を示し、本発明の特徴とする
ところをより一層明瞭にする。EXAMPLES Below, Examples and Comparative Examples will be shown to further clarify the features of the present invention.
第１表には、以下の実施例および比較例で使用した触媒
の金属担持量（酸化物として）および比表面積をあわせ
て示す。Table 1 also shows the amount of metal supported (as an oxide) and specific surface area of the catalysts used in the following Examples and Comparative Examples.
尚、市販の水素化分解用金属担持触媒ＡおよびＢについ
ては、あらかじめ予備硫化を行なった。Note that the commercially available metal-supported catalysts A and B for hydrocracking were pre-sulfided.
実施例１
第１反応器内に触媒Ａ、第２反応器内に触媒Ｃをそれぞ
れ充填して、フェナントレンを原料として、下記の条件
下で軽質化処理を行なった。Example 1 A first reactor was filled with catalyst A, and a second reactor was filled with catalyst C, and a lightening treatment was performed under the following conditions using phenanthrene as a raw material.
第１段 雰囲気ガス 水素
圧力 ７０ｋｇ／ｃＪ
温度 ４００℃
反応時間 ４０分
第２段 雰囲気ガス 水素
圧力 ７０ｋｇ／ｃｊ温度
３５０℃
反応時間 ２０分
軽質化処理した後、得られた生成物とその全体に対する
収量（％）を第２表に示し、析出炭素および転化率を第
３表に示す。1st stage Atmosphere gas Hydrogen pressure 70kg/cJ Temperature 400℃ Reaction time 40 minutes 2nd stage Atmosphere gas Hydrogen pressure 70kg/cJ Temperature
After lightening treatment at 350° C. for 20 minutes, the resulting products and their yields (%) relative to the total are shown in Table 2, and the precipitated carbon and conversion rate are shown in Table 3.
実施例２
第１段反応器内に触媒Ｂ、第２段反応器内に触媒Ｃをそ
れぞれ充填して、フェナントレンを原料として、実施例
１と同様の条件下で軽質化処理を行なった。Example 2 Catalyst B was filled in the first stage reactor, and catalyst C was filled in the second stage reactor, and a lightening treatment was performed under the same conditions as in Example 1 using phenanthrene as a raw material.
軽質化処理した後、得られた生成物とその全体に対する
収量（％）を第２表に示し、析出炭素および転化率を第
３表に示す。After the lightening treatment, the products obtained and their yields (%) relative to the total are shown in Table 2, and the precipitated carbon and conversion rates are shown in Table 3.
比較例１
フェナントレンを原料とし、市販の水素化分解用金属担
持触媒を用いて１段の軽質化処理を行なった。反応条件
は、反応時間が１時間である以外は実施例１の第１段の
反応条件と同様である。Comparative Example 1 Using phenanthrene as a raw material, one stage of lightening treatment was performed using a commercially available metal-supported catalyst for hydrocracking. The reaction conditions are the same as those in the first stage of Example 1, except that the reaction time is 1 hour.
軽質化処理した後、得られた生成物とその全体に対する
収量（％）を第２表に示し、析出炭素および転化率を第
３表に示す。After the lightening treatment, the products obtained and their yields (%) relative to the total are shown in Table 2, and the precipitated carbon and conversion rates are shown in Table 3.
比較例２
フェナントレンを原料とし、金属担持ゼオライト系触媒
を用いて１段の軽質化処理を行なった。Comparative Example 2 Using phenanthrene as a raw material, one stage of lightening treatment was performed using a metal-supported zeolite catalyst.
反応条件は、反応時間が１時間である以外は実施例１の
第１段の反応条件と同様である。The reaction conditions are the same as those in the first stage of Example 1, except that the reaction time is 1 hour.
軽質化処理した後、得られた生成物とその全体に対する
収量（％）を第２表に示し、析出炭素および転化率を第
３表に示す。After the lightening treatment, the products obtained and their yields (%) relative to the total are shown in Table 2, and the precipitated carbon and conversion rates are shown in Table 3.
尚、第２表および第３表中のａ）〜ｄ）は下記の事項を
示す。Note that a) to d) in Tables 2 and 3 indicate the following items.
ａ）ＲＳＲ’ 、Ｒ２は、アルキル基または水素原子で
ある。a) RSR', R2 is an alkyl group or a hydrogen atom.
ｂ）シクロへキシルフェニレンおよびシクロヘキシルベ
ンゼンである。b) cyclohexylphenylene and cyclohexylbenzene.
Ｃ）分子量１８２ （ＧＣ−ＭＳによる）の未確認化合
物を含む。C) Contains an unidentified compound with a molecular weight of 182 (by GC-MS).
ｄ） 触媒上に析出した生成物全体に対する炭素量（％） （燃焼法により測定） である。d) Carbon content (%) based on the total product deposited on the catalyst (Measured by combustion method) It is.
第
表
以上の結果より、本発明の２段接触水素化接触分解によ
れば、第１段反応の反応器内に市販の水素化分解用金属
担持触媒Ｎ ｉ Ｍｏ／Ａ Ｉ ２０３あルイはＣｏＭ
○／Ａｌ□ｏ３、第２段反応の反応器内に分子ふるい作
用をもつ金属担持ゼオライト系触媒を充填した場合には
、フェナントレンの転化率か高（なるだけでなく、有用
な単環および２環芳香族炭化水素の生成が非常に多くな
ることがわかる。From the results in Table 1 and above, according to the two-stage catalytic hydrogenation catalytic cracking of the present invention, the commercially available metal-supported catalyst for hydrogenation N i Mo/A I 203 is CoM in the reactor of the first stage reaction.
○ /Al It can be seen that the generation of ring aromatic hydrocarbons increases significantly.
（以 上）(that's all)
Claims (3)
水素類を含有する重質油を接触分解して軽質化するに際
し、上記２段反応の各反応器内に互いに触媒性能の異な
る触媒を充填し、反応条件をそれぞれ独立に制御するこ
とを特徴とする重質油の接触水素化分解方法。(1) When heavy oil containing polycyclic aromatic hydrocarbons is catalytically cracked and lightened by a two-stage reaction in a hydrogen atmosphere, each reactor in the two-stage reaction has different catalyst performance. A method for catalytic hydrocracking of heavy oil characterized by loading a catalyst and controlling each reaction condition independently.
第１段反応の反応器内に充填する特許請求の範囲第１項
記載の重質油の接触水素化分解方法。(2) The method for catalytic hydrocracking of heavy oil according to claim 1, wherein a supported metal catalyst for hydrocracking having an appropriate acidity is packed into a reactor for the first stage reaction.
ン交換に供することにより得られる金属担持ゼオライト
を第２段反応の反応器内に充填する特許請求の範囲第１
項記載の重質油の接触水素化分解方法。(3) Claim 1, in which a metal-supported zeolite obtained by subjecting ammonium ion-substituted Y-zeolite to ion exchange is filled into a reactor for the second stage reaction.
A method for catalytic hydrocracking of heavy oil as described in .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24418390A JPH04122789A (en) | 1990-09-14 | 1990-09-14 | Catalytic hydrocracking of heavy oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24418390A JPH04122789A (en) | 1990-09-14 | 1990-09-14 | Catalytic hydrocracking of heavy oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04122789A true JPH04122789A (en) | 1992-04-23 |
Family
ID=17115004
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP24418390A Pending JPH04122789A (en) | 1990-09-14 | 1990-09-14 | Catalytic hydrocracking of heavy oil |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04122789A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100348702C (en) * | 2005-10-28 | 2007-11-14 | 中国石油化工集团公司 | Process for producing fuel oil |
| CN106582456A (en) * | 2015-10-14 | 2017-04-26 | 中国石油化工股份有限公司 | Composite hydrogenation catalyst bed |
| CN110538676A (en) * | 2018-05-29 | 2019-12-06 | 中国石油化工股份有限公司 | Catalyst for hydrogenation refining of cracked tar |
| CN110538659A (en) * | 2018-05-29 | 2019-12-06 | 中国石油化工股份有限公司 | Catalyst for refining cracked tar |
-
1990
- 1990-09-14 JP JP24418390A patent/JPH04122789A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100348702C (en) * | 2005-10-28 | 2007-11-14 | 中国石油化工集团公司 | Process for producing fuel oil |
| CN106582456A (en) * | 2015-10-14 | 2017-04-26 | 中国石油化工股份有限公司 | Composite hydrogenation catalyst bed |
| CN110538676A (en) * | 2018-05-29 | 2019-12-06 | 中国石油化工股份有限公司 | Catalyst for hydrogenation refining of cracked tar |
| CN110538659A (en) * | 2018-05-29 | 2019-12-06 | 中国石油化工股份有限公司 | Catalyst for refining cracked tar |
| CN110538659B (en) * | 2018-05-29 | 2021-12-28 | 中国石油化工股份有限公司 | Catalyst for refining cracked tar |
| CN110538676B (en) * | 2018-05-29 | 2021-12-28 | 中国石油化工股份有限公司 | Catalyst for hydrogenation refining of cracked tar |
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