JPH07102267A - Method for improving hue of hydrotreated oil - Google Patents
Method for improving hue of hydrotreated oilInfo
- Publication number
- JPH07102267A JPH07102267A JP31121993A JP31121993A JPH07102267A JP H07102267 A JPH07102267 A JP H07102267A JP 31121993 A JP31121993 A JP 31121993A JP 31121993 A JP31121993 A JP 31121993A JP H07102267 A JPH07102267 A JP H07102267A
- Authority
- JP
- Japan
- Prior art keywords
- hue
- oil
- hydrotreated
- hydrotreated oil
- sulfur content
- 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
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、色相の悪い水素化処理
油の色相改善方法に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for improving the hue of a hydrotreated oil having a poor hue.
【０００２】[0002]
【従来の技術】石油蒸留物を高品質化するために、水素
化処理によりその中に含まれるイオウ分を除去すること
は知られている。この水素化処理は、従来は、４０ｋｇ
／ｃｍ2以下の圧力下、３００℃より低い一定温度条件
で行われている。しかし、このような従来の水素化処理
では、その低イオウ化には限界があり、脱硫率を向上さ
せるために反応温度を上げると、得られる水素化処理油
の色相が著しく悪化するという問題があった。In order to improve the quality of petroleum distillates, it is known to remove the sulfur content contained therein by hydrotreating. This hydrotreatment is conventionally 40 kg
It is carried out under a constant temperature condition of lower than 300 ° C. under a pressure of / cm 2 or less. However, in such a conventional hydrotreatment, there is a limit to the reduction of sulfur, and when the reaction temperature is raised to improve the desulfurization rate, the hue of the hydrotreated oil obtained is significantly deteriorated. there were.
【０００３】[0003]
【発明が解決しようとする課題】本発明は、石油蒸留物
の水素化処理により得られる色相の悪化した水素化処理
油の色相改善方法を提供することをその課題とする。SUMMARY OF THE INVENTION An object of the present invention is to provide a method for improving the hue of a hydrotreated oil obtained by hydrotreating a petroleum distillate and having a deteriorated hue.
【０００４】[0004]
【課題を解決するための手段】本発明者らは、前記課題
を解決するために、種々研究を重ねた結果、本発明を完
成するに至った。すなわち、本発明によれば、石油蒸留
物の水素化処理油であって、イオウ分が０．４重量％以
下でかつ色相悪化物質を含有するセイボルトカラー値が
−１５以下の色相の悪い水素化処理油を、水素化処理触
媒の存在下で水素化処理して、該油中に含まれる色相悪
化物質を水素化し、セイボルトカラー値が＋１５以上の
色相の良好な水素化処理油に変換させることを特徴とす
る色相悪化した水素化処理油の色相改善方法が提供され
る。Means for Solving the Problems The present inventors have completed the present invention as a result of various studies in order to solve the above problems. That is, according to the present invention, a hydrotreated oil of a petroleum distillate, which has a sulfur content of 0.4% by weight or less and contains a hue deteriorating substance and has a Saybolt color value of -15 or less and a bad hue. The hydrogenated oil is hydrotreated in the presence of a hydrotreating catalyst to hydrogenate a hue deteriorating substance contained in the oil and convert it into a hydrotreated oil having a good Saybolt color value of +15 or more. A method for improving the hue of a hydrotreated oil having a deteriorated hue is provided.
【０００５】石油蒸留物を、その中に含まれているイオ
ウ分を除去するために、水素化処理する場合、その脱硫
率は水素化処理温度と関係し、水素化処理温度を高める
ことにより脱硫率を増加させることができ、得られる水
素化処理油中のイオウ分も低くなる。しかし、このよう
にして石油蒸留物中のイオウ分を低減させる場合、得ら
れる水素化処理油は、イオウ分の低減されたものではあ
るが、逆に、その水素化処理油中には、その高温の水素
化処理により副生する色相悪化物質が含まれるようにな
り、その水素化処理油の色相は悪化する。従って、従来
は、このような色相悪化を生じないような条件で水素化
処理を行っていたため、石油蒸留物中のイオウ分の低減
化には限度があった。本発明者らは、このような低イオ
ウ分ではあるが色相悪化物質を含む色相の悪い水素化処
理油は、これを水素化処理することにより、その色相を
効果的に改善し得ることを見出し、この知見に基づいて
本発明を完成したものである。When a petroleum distillate is hydrotreated in order to remove the sulfur content contained therein, the desulfurization rate thereof is related to the hydrotreating temperature, and desulfurization is performed by increasing the hydrotreating temperature. The rate can be increased and the sulfur content in the resulting hydrotreated oil will also be low. However, in the case of reducing the sulfur content in the petroleum distillate in this manner, the hydrotreated oil obtained is the one in which the sulfur content is reduced, but conversely, in the hydrotreated oil, Hue-treating substances produced as a by-product due to the high-temperature hydrotreatment are contained, and the hue of the hydrotreated oil deteriorates. Therefore, conventionally, the hydrogenation treatment has been carried out under such a condition as not to cause such deterioration of hue, so that there is a limit to the reduction of the sulfur content in the petroleum distillate. The present inventors have found that a hydrotreated oil having such a low sulfur content but a poor hue including a hue deteriorating substance can effectively improve its hue by hydrotreating it. The present invention has been completed based on this finding.
【０００６】本発明の色相改善方法で対象とする原料水
素化処理油は、イオウ分が０．４重量％以下と低イオウ
分であるが、色相悪化物質を含み、そのセイボルトカラ
ー値が−１５以下の色相の著しく悪い水素化処理油であ
る。本発明によれば、このような水素化処理油は、これ
を水素化処理し、その油中に含まれる色相悪化物質を水
素化することにより、その水素化処理油の色相を改善す
ることができる。The raw hydrotreated oil which is the object of the hue improving method of the present invention has a low sulfur content of 0.4% by weight or less, but contains a hue degrading substance and has a Saybolt color value of −. It is a hydrotreated oil having a hue of 15 or less, which is extremely poor. According to the present invention, such a hydrotreated oil is capable of improving the hue of the hydrotreated oil by hydrotreating the hydrotreated oil and hydrogenating the hue deteriorating substance contained in the oil. it can.
【０００７】本発明による色相悪化物質を含む水素化処
理油の水素化処理工程は、その原料水素化処理油中に含
まれる色相悪化物質を水素化し、セイボルトカラー値が
１５以上に高められた水素化処理油が得られるように実
施される。原料水素化処理油中に含まれる色相悪化物質
は、本来、石油蒸留物中には含まれていないもので、石
油蒸留物を高脱硫率で水素化処理する際に新しく生成し
たもので、芳香族化合物の重縮合物と考えられる。本発
明により原料水素化処理油の色相が改善される理由は、
この芳香族化合物の重縮合物が核水素化され、着色のな
い色相安定な水素化物に転換されることによるものと考
えられる。In the hydrotreating step of the hydrotreated oil containing the hue deteriorating substance according to the present invention, the hue deteriorating substance contained in the raw hydrotreated oil was hydrogenated to increase the Saybolt color value to 15 or more. It is carried out so as to obtain a hydrotreated oil. Hue-deteriorating substances contained in the raw hydrotreated oil were originally not contained in petroleum distillates, and were newly produced when hydrotreating petroleum distillates at a high desulfurization rate. It is considered to be a polycondensate of a group compound. The reason why the hue of the raw hydrotreated oil is improved by the present invention is
It is thought that this is because the polycondensate of the aromatic compound is nuclear-hydrogenated and converted into a hydride that is stable and has no color.
【０００８】この水素化処理工程における反応温度は、
通常、１５０〜３２５℃、好ましくは２００〜３００℃
であり、圧力は、通常、５〜４０ｋｇ／ｃｍ2、好まし
くは１０〜３０ｋｇ／ｃｍ2である。液空間速度（ＬＨ
ＳＶ）は、通常、０．５〜５．０ｈｒ-1、好ましくは
２．０〜４．０ｈｒ-1であり、水素ガス／原料油比率
は、通常、５０〜４５０ｍ3／ｋｌ、好ましくは８０〜
１６０ｍ3／ｋｌである。水素化処理触媒としては、従
来公知のもの、例えば、多孔性担体に、Ｖ，Ｍｏ，Ｗ，
Ｎｉ，Ｃｏ，Ｐｄ，Ｐｔ，Ｒｅ，Ｒｕ，Ｒｈ等の水素化
活性金属種を担持させたものが用いられる。多孔性担体
としては、アルミナ、シリカ、チタニア、アルミナシリ
カ、アルミナチタニア、アルミナジルコニア、シリカマ
グネシア等が用いられる。特に、アルミナに担持させた
Ｎｉ−Ｍｏ、Ｃｏ−Ｍｏ、Ｎｉ−Ｃｏ−Ｍｏ、Ｎｉ−Ｗ
等の触媒の使用が好ましい。The reaction temperature in this hydrotreating step is
Usually, 150 to 325 ° C, preferably 200 to 300 ° C
And the pressure is usually 5 to 40 kg / cm 2 , preferably 10 to 30 kg / cm 2 . Liquid space velocity (LH
SV) is usually 0.5 to 5.0 hr -1 , preferably 2.0 to 4.0 hr -1 , and the hydrogen gas / feed oil ratio is usually 50 to 450 m 3 / kl, preferably 80. ~
It is 160 m 3 / kl. Conventionally known hydrotreating catalysts include, for example, V, Mo, W, and
A material carrying a hydrogenation-active metal species such as Ni, Co, Pd, Pt, Re, Ru, Rh is used. As the porous carrier, alumina, silica, titania, alumina silica, alumina titania, alumina zirconia, silica magnesia, etc. are used. In particular, Ni-Mo, Co-Mo, Ni-Co-Mo, Ni-W supported on alumina
The use of catalysts such as
【０００９】この水素化処理工程では、被処理原料とし
て用いる色相の悪い水素化処理油の色相改善を達成すれ
ばよいことから、水素化処理油のイオウ分を格別減少さ
せる必要はなく、得られる製品水素化処理油中のイオウ
分は実質上原料水素化処理油のイオウ分と同じであるこ
とができる。従って、この場合には、水素化処理工程
は、イオウ分の格別の除去を要しないことから、コンパ
クトな装置を用いて実施することができる。もちろん、
必要に応じ、この水素化処理工程で、原料水素化処理油
のイオウ分を相当程度除去することも可能である。この
水素化処理工程で得られた生成物は、これを気液分離し
た後、得られた水素化処理油をストリッピングして、そ
の中に含まれる軽質留分を分離して製品水素化処理油と
して回収される。In this hydrotreatment step, since it is sufficient to achieve the improvement of the hue of the hydrotreated oil having a poor hue used as the raw material to be treated, it is not necessary to reduce the sulfur content of the hydrotreated oil, and it is obtained. The sulfur content in the product hydrotreated oil can be substantially the same as the sulfur content in the feed hydrotreated oil. Therefore, in this case, the hydrotreating step does not require any special removal of the sulfur content, and therefore can be carried out using a compact apparatus. of course,
If necessary, it is possible to considerably remove the sulfur content of the feedstock hydrotreated oil in this hydrotreatment step. The product obtained in this hydroprocessing step is gas-liquid separated, and then the resulting hydrotreated oil is stripped to separate the light fractions contained in the product and the product hydrotreated. Recovered as oil.
【００１０】本発明で被処理原料油として用いる水素化
処理油は、石油蒸留物を水素化処理して得られたもので
あるが、この場合の石油蒸留物としては、例えば、原油
の常圧又は減圧蒸留により得られる蒸留物の他、流動接
触分解（ＦＣＣ）油の蒸留物、熱分解油の蒸留物等が挙
げられる。これらの石油蒸留物は単独又は混合物の形で
用いられる。本発明で用いる好ましいものは、自動車軽
油として使用される石油蒸留物であり、１５０〜３７０
℃の蒸留性状を有するものである。これらの石油蒸留物
は、イオウ分を含み、そのイオウ分は、通常、０．８〜
１．２重量％の範囲にある。もちろん、石油蒸留物によ
っては、前記範囲よりイオウ分の多いものや、少ないも
のがあるが、本発明で用いる石油蒸留物は、このような
石油蒸留物であってもよい。The hydrotreated oil used as the raw material oil to be treated in the present invention is obtained by hydrotreating petroleum distillate. The petroleum distillate in this case is, for example, the normal pressure of crude oil. In addition to distillates obtained by distillation under reduced pressure, distillates of fluid catalytic cracking (FCC) oil, distillates of pyrolysis oil, and the like can be mentioned. These petroleum distillates are used alone or in the form of a mixture. The preferred one used in the present invention is a petroleum distillate used as an automobile gas oil, which is 150 to 370.
It has a distillation property of ° C. These petroleum distillates contain a sulfur content, which is usually between 0.8 and
It is in the range of 1.2% by weight. Of course, depending on the petroleum distillate, there are those having a sulfur content higher or lower than the above range, but the petroleum distillate used in the present invention may be such a petroleum distillate.
【００１１】石油蒸留物の水素化処理は、その中に含ま
れているイオウ分を高い脱硫率で除去するために行われ
るものであり、前記した色相改善のための水素化処理工
程の温度よりも高い温度条件が採用される。この石油蒸
留物の水素化処理工程における反応温度は、通常、２８
０〜３７０℃、好ましくは３３０〜３６０℃であり、圧
力は、通常、５〜４０ｋｇ／ｃｍ2、好ましくは１０〜
３０ｋｇ／ｃｍ2である。液空間速度（ＬＨＳＶ）は、
通常、０．５〜５．０ｈｒ-1、好ましくは２．０〜４．
０ｈｒ-1であり、水素ガス／原料油比率は、通常、５０
〜４５０ｍ3／ｋｌ、好ましくは８０〜１６０ｍ3／ｋｌ
である。水素化処理触媒としては、従来公知のもの、例
えば、多孔性担体に、Ｖ，Ｍｏ，Ｗ，Ｎｉ，Ｃｏ，Ｐ
ｄ，Ｐｔ，Ｒｅ，Ｒｕ，Ｒｈ等の水素化活性金属種を担
持させたものが用いられる。多孔性担体としては、アル
ミナ、シリカ、チタニア、アルミナシリカ、アルミナチ
タニア、アルミナジルコニア、シリカマグネシア等が用
いられる。特に、アルミナに担持させたＮｉ−Ｍｏ、Ｃ
ｏ−Ｍｏ、Ｎｉ−Ｃｏ−Ｍｏ、Ｎｉ−Ｗ等の触媒の使用
が好ましい。The hydrotreatment of petroleum distillates is carried out in order to remove the sulfur content contained therein at a high desulfurization rate. Also high temperature conditions are adopted. The reaction temperature in the hydrotreating process of this petroleum distillate is usually 28.
0 to 370 ° C., preferably 330 to 360 ° C., the pressure is usually 5 to 40 kg / cm 2 , preferably 10 to
It is 30 kg / cm 2 . Liquid hourly space velocity (LHSV) is
Usually, it is 0.5 to 5.0 hr -1 , preferably 2.0 to 4.
0 hr -1 , and the hydrogen gas / feed oil ratio is usually 50
~ 450 m 3 / kl, preferably 80-160 m 3 / kl
Is. As the hydrotreating catalyst, a conventionally known catalyst, for example, V, Mo, W, Ni, Co, P on a porous carrier is used.
A material carrying a hydrogenation active metal species such as d, Pt, Re, Ru, Rh is used. As the porous carrier, alumina, silica, titania, alumina silica, alumina titania, alumina zirconia, silica magnesia, etc. are used. In particular, Ni-Mo, C supported on alumina
The use of catalysts such as o-Mo, Ni-Co-Mo, Ni-W is preferred.
【００１２】この石油蒸留物の水素化処理工程において
は、石油蒸留物中のイオウ分が高率で除去される。この
石油蒸留物の水素化処理工程は、得られる水素化処理油
中のイオウ分が０．４重量％以下、特に、０．２重量％
以下、必要に応じてさらに低いイオウ分になるように実
施される。このイオウ分の除去は、水素化処理温度を高
くすることにより効率よく行うことができる。このよう
にして石油蒸留物の水素化処理により得られる水素化処
理油は、石油蒸留物を高率で脱硫したために、副生した
色相悪化物質を含むもので、その色相は、セイボルトカ
ラー値で、−１５以下と著しく悪化されたものである。In the hydrotreating process of this petroleum distillate, the sulfur content in the petroleum distillate is removed at a high rate. In the hydrotreating process of this petroleum distillate, the sulfur content in the hydrotreated oil obtained is 0.4% by weight or less, particularly 0.2% by weight.
Hereinafter, if necessary, it is carried out so as to obtain a lower sulfur content. The removal of the sulfur content can be efficiently performed by increasing the hydrotreatment temperature. The hydrotreated oil thus obtained by the hydrotreatment of petroleum distillate contains a substance that deteriorates in hue due to desulfurization of petroleum distillate at a high rate, and its hue is the Saybolt color value. Then, it was significantly deteriorated to -15 or less.
【００１３】次に、本発明の好ましい実施態様につい
て、図面により説明する。図１は本発明の１つの好まし
い実施態様についてのフローシートを示す。図１におい
て、１及び２は反応器、３は加熱炉、５は熱交換器、６
は気液分離器を示す。図１において、石油蒸留物はライ
ン８及びポンプ４を通り、さらに熱交換器５を通って、
ライン９からの水素ガスとともに加熱炉３に導入され、
ここで所定温度に加熱された後、第１反応器１に導入さ
れ、第１段階の水素化処理を受ける。反応器１からライ
ン１４を通って抜出された色相の悪い第１水素化処理油
と水素ガスとの混合物は、熱交換器５を通り、ここで石
油蒸留物との間で熱交換され、所定の温度まで冷却され
た後、第２反応器２に導入され、本発明による第２段階
の水素化処理を受ける。第２反応器２からライン１５を
通って抜出された第２水素化処理油と水素ガスの混合物
は、気液分離器６に導入され、ここで気液分離され、分
離されたガス成分はオフガスとしてライン１０を通って
排出される。一方、第２水素化処理油は、ライン１１を
通ってストリッパー７に導入され、ここで軽質分がライ
ン１２を通って分離され、製品として第２水素化処理油
がライン１３を通って回収される。Next, preferred embodiments of the present invention will be described with reference to the drawings. FIG. 1 shows a flow sheet for one preferred embodiment of the present invention. In FIG. 1, 1 and 2 are reactors, 3 is a heating furnace, 5 is a heat exchanger, and 6
Indicates a gas-liquid separator. In FIG. 1, the petroleum distillate passes through line 8 and pump 4, and then through heat exchanger 5,
Introduced into the heating furnace 3 together with hydrogen gas from line 9,
Here, after being heated to a predetermined temperature, it is introduced into the first reactor 1 and subjected to the first stage hydrogenation treatment. The mixture of the poorly colored first hydrotreated oil and hydrogen gas withdrawn from reactor 1 through line 14 passes through heat exchanger 5 where it is heat exchanged with petroleum distillates, After being cooled to a predetermined temperature, it is introduced into the second reactor 2 and subjected to the second stage hydrotreatment according to the present invention. The mixture of the second hydrotreated oil and hydrogen gas extracted from the second reactor 2 through the line 15 is introduced into the gas-liquid separator 6, where it is gas-liquid separated, and the separated gas component is It is discharged as off-gas through the line 10. On the other hand, the second hydrotreated oil is introduced into the stripper 7 through the line 11, where the light component is separated through the line 12, and the second hydrotreated oil is recovered as a product through the line 13. It
【００１４】図２は本発明の好ましい他の実施態様につ
いてのフローシートを示す。図２において、石油蒸留物
はライン８及びポンプ４を通ってライン９からの水素ガ
スとともに加熱炉３に導入され、ここで所定温度に加熱
された後、第１反応器１に導入され、第１段階の水素化
処理を受ける。反応器１からライン１４を通って抜出さ
れた色相の悪い第１水素化処理油と水素ガスとの混合物
は、循環ライン２１を通って循環される低温の第２水素
化処理油と混合され、さらにライン２０からのクエンチ
用水素ガスと混合されて所定の温度まで冷却された後、
第２反応器２に導入され、本発明による第２段階の水素
化処理を受ける。第２反応器からライン１５を通って抜
出された第２水素化処理油と水素ガスとの混合物は、図
１に示した場合と同様にして後処理される。FIG. 2 shows a flow sheet for another preferred embodiment of the present invention. In FIG. 2, the petroleum distillate is introduced into the heating furnace 3 through the line 8 and the pump 4 together with the hydrogen gas from the line 9, where it is heated to a predetermined temperature and then introduced into the first reactor 1. It undergoes a one-stage hydrotreatment. The mixture of the first hydrotreated oil having a bad hue and hydrogen gas extracted from the reactor 1 through the line 14 is mixed with the low temperature second hydrotreated oil circulated through the circulation line 21. , Further mixed with quenching hydrogen gas from line 20 and cooled to a predetermined temperature,
It is introduced into the second reactor 2 and undergoes the second stage hydrotreatment according to the present invention. The mixture of the second hydrotreated oil and hydrogen gas withdrawn from the second reactor through the line 15 is post-treated in the same manner as shown in FIG.
【００１５】[0015]
【発明の効果】本発明によれば、石油蒸留物の水素化処
理により得られる、低イオウ分であるが色相の悪い水素
化処理油の色相を効果的に改善することができる。本発
明により得られる低イオウ分でかつ色相の良好な製品水
素化処理油は、自動車用軽油として有利に使用される。According to the present invention, it is possible to effectively improve the hue of a hydrotreated oil having a low sulfur content but a poor hue, which is obtained by the hydrotreatment of a petroleum distillate. The product hydrotreated oil having a low sulfur content and a good hue obtained by the present invention is advantageously used as a light oil for automobiles.
【００１６】[0016]
【実施例】次に本発明を実施例によりさらに詳細に説明
する。EXAMPLES Next, the present invention will be described in more detail by way of examples.
【００１７】実施例１〜２、比較例１〜２ 石油蒸留物として、直留軽油９０重量％と分解軽油１０
重量％との混合油を用いた。この混合油の比重（１５／
４℃）は０．８５３であり、イオウ分を１．０６重量％
含有するものであった。また、この混合油の蒸留開始点
は２０２℃であり、蒸留終点は３６２℃であった。前記
石油蒸留物を図１に示したフローに従って２段階の水素
化処理に付した。その処理条件と処理結果を表１に示
す。また、比較のために、原料油を１段階の水素化処理
により処理した結果もあわせて表１に示す。Examples 1-2, Comparative Examples 1-2 As petroleum distillates, 90% by weight of straight-run light oil and 10 of cracked light oil were used.
A mixed oil with wt% was used. Specific gravity of this mixed oil (15 /
4 ° C) is 0.853 and the sulfur content is 1.06% by weight.
It was contained. The distillation start point of this mixed oil was 202 ° C, and the distillation end point was 362 ° C. The petroleum distillate was subjected to a two-stage hydrotreatment according to the flow shown in FIG. Table 1 shows the processing conditions and the processing results. In addition, for comparison, Table 1 also shows the results obtained by treating the feedstock with one-stage hydrotreatment.
【００１８】[0018]
【表１】 *1…原料油１ｋｌ当りのＨ2ガス量（ｍ3） *2…単位触媒容積に対する原料油の流量比(ｈｒ-1)[Table 1] * 1… Amount of H 2 gas per 1 kl of feed oil (m 3 ) * 2… Ratio of feed oil flow rate per unit catalyst volume (hr −1 )
【００１９】表１に示した実験結果からわかるように、
本発明による実施例１及び実施例２では、最終的に得ら
れる処理油のイオウ分は低くかつ色相も良好である。こ
れに対し、比較例１では、実施例１及び２と同レベルの
低イオウ化処理油を得るには、通油量を著しく小さくす
る必要があるため、原料油の時間当りの処理効果が悪
く、しかも処理油の色相も悪い。比較例２は、反応温度
を高くして、通油量を実施例１及び実施例２と同じレベ
ルにして低イオウ化処理油を得るものであるが、この場
合には、得られる水素化処理油の色相は非常に悪いもの
となる。As can be seen from the experimental results shown in Table 1,
In Examples 1 and 2 according to the present invention, the finally obtained treated oil has a low sulfur content and a good hue. On the other hand, in Comparative Example 1, in order to obtain a low-sulfurized oil having the same level as in Examples 1 and 2, it was necessary to significantly reduce the amount of oil to be passed, so that the effect of treating the feed oil per hour was poor. Moreover, the hue of the treated oil is also poor. In Comparative Example 2, the reaction temperature was raised and the amount of oil passed was set to the same level as in Examples 1 and 2 to obtain a low-sulfurized oil. In this case, however, the obtained hydrotreated oil was used. The hue of the oil will be very poor.
【図１】図１は本発明の１つの実施態様についてのフロ
ーシートを示す。FIG. 1 shows a flow sheet for one embodiment of the present invention.
【図２】図２は本発明の他の実施態様についてのフロー
シートを示す。FIG. 2 shows a flow sheet for another embodiment of the present invention.
１，２ 反応器 ３ 加熱炉 ５ 熱交換器 ６ 気液分離器 ７ ストリッパー 1, 2 Reactor 3 Heating furnace 5 Heat exchanger 6 Gas-liquid separator 7 Stripper
Claims (3)
オウ分が０．４重量％以下でかつ色相悪化物質を含有す
るセイボルトカラー値が−１５以下の色相の悪い水素化
処理油を、水素化処理触媒の存在下で水素化処理して、
該油中に含まれる色相悪化物質を水素化し、セイボルト
カラー値が＋１５以上の色相の良好な水素化処理油に変
換させることを特徴とする色相悪化した水素化処理油の
色相改善方法。1. A hydrotreated oil for petroleum distillates, having a sulfur content of 0.4% by weight or less and a Saybolt color value of -15 or less, containing a hue deteriorating substance and having a bad hue. Is hydrotreated in the presence of a hydrotreating catalyst,
A method for improving a hue of a hydrotreated oil having a deteriorated hue, which comprises hydrogenating a hue deteriorating substance contained in the oil and converting the same to a hydrotreated oil having a good Saybolt color value of +15 or more.
力が１０〜４０ｋｇ／ｃｍ2である請求項１の方法。 2. The method according to claim 1, wherein the hydrotreating temperature is 150 to 325 ° C. and the pressure is 10 to 40 kg / cm 2 .
色相の悪い水素化処理油のイオウ分と実質上同じである
請求項１又は２の方法。3. A process according to claim 1, wherein the hydrotreated oil having a good hue has a sulfur content substantially the same as that of a hydrotreated oil having a bad hue.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP31121993A JPH07102267A (en) | 1993-11-17 | 1993-11-17 | Method for improving hue of hydrotreated oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP31121993A JPH07102267A (en) | 1993-11-17 | 1993-11-17 | Method for improving hue of hydrotreated oil |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1223078A Division JP2530498B2 (en) | 1989-08-31 | 1989-08-31 | Method for reducing sulfur in petroleum distillates |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH07102267A true JPH07102267A (en) | 1995-04-18 |
Family
ID=18014539
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP31121993A Pending JPH07102267A (en) | 1993-11-17 | 1993-11-17 | Method for improving hue of hydrotreated oil |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH07102267A (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0386793A (en) * | 1989-08-31 | 1991-04-11 | Tonen Corp | Method for decreasing sulfur content of petroleum distillate |
-
1993
- 1993-11-17 JP JP31121993A patent/JPH07102267A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0386793A (en) * | 1989-08-31 | 1991-04-11 | Tonen Corp | Method for decreasing sulfur content of petroleum distillate |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4149965A (en) | Method for starting-up a naphtha hydrorefining process | |
| JP2966985B2 (en) | Catalytic hydrotreating method for heavy hydrocarbon oil | |
| US5871636A (en) | Catalytic reduction of acidity of crude oils in the absence of hydrogen | |
| US5316658A (en) | Process for the production of low-sulfur diesel gas oil | |
| US5906729A (en) | Process scheme for processing sour feed in isomerization dewaxing | |
| CN108728162B (en) | Method for producing raw material rich in monocyclic aromatic hydrocarbon | |
| CN108795495B (en) | Method for treating diesel raw material | |
| JP2530498B2 (en) | Method for reducing sulfur in petroleum distillates | |
| JP2002513848A (en) | Multi-stage hydrotreatment of middle distillates to avoid hue bodies | |
| US4973396A (en) | Method of producing sweet feed in low pressure hydrotreaters | |
| JPH07102266A (en) | Process for reducing sulfur content of petroleum distillate | |
| JP2863326B2 (en) | Crude oil refining method | |
| JPH07102267A (en) | Method for improving hue of hydrotreated oil | |
| JP3634041B2 (en) | Light oil quality treatment method | |
| CN1382775A (en) | Process for preparing light fuel oil and basic oil of lubricant at same time | |
| CN101942328B (en) | Hydrogenation method for gasoline and diesel | |
| JPH05112785A (en) | Treatment of heavy hydrocarbon oil | |
| JPH07300592A (en) | Method of treating petroleum | |
| JP2530498C (en) | ||
| JP2799421B2 (en) | Operating method of hydrotreating equipment | |
| JPH05239472A (en) | Method of processing heavy hydrocarbon oil | |
| JPH08183964A (en) | Hydrogenative treatment of feedstock for fluid-bed catalytic cracking | |
| CN116064112A (en) | Jet fuel composition and preparation method thereof | |
| JP2000212578A (en) | Production of low sulfur light oil and light oil composition prepared thereby | |
| JP4700153B2 (en) | Fuel oil |