JPH0386793A - Method for decreasing sulfur content of petroleum distillate - Google Patents
Method for decreasing sulfur content of petroleum distillateInfo
- Publication number
- JPH0386793A JPH0386793A JP1223078A JP22307889A JPH0386793A JP H0386793 A JPH0386793 A JP H0386793A JP 1223078 A JP1223078 A JP 1223078A JP 22307889 A JP22307889 A JP 22307889A JP H0386793 A JPH0386793 A JP H0386793A
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- sulfur content
- temperature
- hydrogenation
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Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
（技術分野）
本発明は、石油蒸留物の低イオウ化方法に関するもので
ある。DETAILED DESCRIPTION OF THE INVENTION (Technical Field) The present invention relates to a method for reducing the sulfur content of petroleum distillates.
（従来技術及びその問題点）
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／ａｉ以下の圧
力下、３００℃より低い一定温度条件で行われている。(Prior art and its problems) It is known that in order to improve the quality of petroleum distillates, the sulfur content contained therein is removed by hydrotreating. This hydrogenation treatment has conventionally been carried out under a pressure of 40 kg/ai or less and at a constant temperature lower than 300°C.
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、得られる処理油の色相が著しく悪化する
という問題があった。However, such conventional hydrotreating has a limit to its low sulfurization, and when the reaction temperature is raised to improve the desulfurization rate, the hue of the resulting treated oil deteriorates significantly. .
（発明の課題）
本発明は、従来の技術に見られる前記問題を解決し１石
油蒸留物を色相の悪化を伴わずに低イオウ化する方法を
提供することをその課題とする。(Problem of the Invention) An object of the present invention is to provide a method for solving the above-mentioned problems seen in the conventional techniques and reducing the sulfur content of a petroleum distillate without deteriorating the hue.
（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１種々研究を
重ねた結果１本発明を完成するに至った。(Means for Solving the Problems) In order to solve the above problems, the present inventors have conducted various studies and have completed the present invention.
すなわち、本発明によれば、イオウ分を０．８〜１゜２
重量ガ含む石油蒸留物を水素化処理触媒の存在下で２段
階で水素化処理することからなり、第１段階の水素化処
理を温度２８０〜３７０℃、圧力１０〜４０ｋｇ／ｃｄ
の条件下でイオウ分が０．４重量％以下になるように行
ない、第２段の水素化処理を第１段階の水素化処理温度
よりも低く、温度１５０〜３２５℃、圧力１０−４０ｋ
ｇ／ｃｍ２の条件下でセイボルトカラー値が０以上にな
るように行うことを特徴とする石油蒸留物の低イオウ化
方法が提供される。That is, according to the present invention, the sulfur content is reduced to 0.8 to 1°2.
It consists of hydrotreating a petroleum distillate containing heavy gas in two stages in the presence of a hydrotreating catalyst, and the first stage hydrotreating is carried out at a temperature of 280 to 370°C and a pressure of 10 to 40 kg/cd.
The second stage hydrogenation treatment was carried out under the following conditions so that the sulfur content was 0.4% by weight or less, and the second stage hydrogenation was carried out at a temperature lower than the first stage hydrogenation temperature, at a temperature of 150 to 325°C and a pressure of 10 to 40K.
There is provided a method for reducing the sulfur content of a petroleum distillate, which is carried out under conditions of g/cm2 such that the Saybolt color value is 0 or more.
本発明で用いる原料油は石油蒸留物であり、原油の常圧
又は減圧蒸留により得られる蒸留物の他。The raw material oil used in the present invention is a petroleum distillate, including distillates obtained by normal pressure or vacuum distillation of crude oil.
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０本発明で用いる好ましい原料油は、
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、通常、０．８−１．２重量２のイオウ分を
含有するものである。Distillates of fluid catalytic cracking (FCC) oils, distillates of pyrolysis oils, and the like can be mentioned. These petroleum distillates may be used alone or in the form of mixtures. Preferred feedstock oils used in the present invention are:
It is a petroleum distillate used as automobile diesel oil, and has a 150%
It has distillation properties of ~370°C. These petroleum distillates usually contain 0.8-1.2 parts by weight of sulfur.
本発明によれば、原料油は、２つの異った温度条件の水
素化処理段階（２段階水素化処理）で処理される。すな
わち、第１段階の水素化処理では、２８０−３７０℃、
好ましくは３３０〜３６０℃の温度条件が採用され、第
２段階の水素化処理では、第１段階の水素化処理温度よ
り低められた温度で、１５０−３２５℃、好ましくは２
００〜３００℃の温度条件が採用される。According to the invention, the feedstock is treated in two hydrotreating stages at different temperature conditions (two-stage hydrotreating). That is, in the first stage hydrogenation treatment, the temperature is 280-370°C,
Preferably, a temperature condition of 330-360°C is adopted, and in the second stage hydrogenation treatment, the temperature is lowered than the first stage hydrogenation temperature, at a temperature of 150-325°C, preferably 2.
Temperature conditions of 00-300°C are employed.
このような２段階の水素化処理により、処理油の色相を
悪化させずに１石油蒸留物の効果的な低イオウ化を達成
することができる。Such two-stage hydrogenation treatment makes it possible to effectively reduce the sulfur content of a petroleum distillate without deteriorating the hue of the treated oil.
次に１本発明で用いる各段階の水素化条件について説明
する。Next, the hydrogenation conditions of each stage used in the present invention will be explained.
（第１段階）
第１段階の水素化処理温度は、２８０〜３７０℃、好ま
しくは３３０〜３６０℃であり、圧力は５−４０ｋｇ／
ｃＪ、好ましくは１０−３０ｋｇ／ｃｍ２ テある。液
空間速度（ＬＩＩＳＶ）は０．５〜５．０ｈｒ−’、好
ましくは２．０−４．０ｈｒ−１であり、水素ガス１Ｍ
料油比率は５０〜４５０ｎ？／ＩＱ、好ましくは８Ｏ−
１６Ｏｎ？／ｋｎ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、Ｖ、
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−Ｎｏ％Ｃｏ−Ｍｏ、Ｎｉ−Ｃｏ−Ｎｏ、Ｎ１−Ｖ
等の触媒の使用が好ましい。(First stage) The hydrogenation temperature in the first stage is 280 to 370°C, preferably 330 to 360°C, and the pressure is 5 to 40 kg/
cJ, preferably 10-30 kg/cm2. Liquid hourly space velocity (LIISV) is 0.5-5.0 hr-', preferably 2.0-4.0 hr-1, and hydrogen gas 1M
Is the oil ratio 50 to 450n? /IQ, preferably 8O-
16On? /kn. Hydrotreating catalysts include conventionally known catalysts, such as V, Mo, V,
Those on which hydrogenation active metal species such as Ni, Co, Pd, Pt, Re, Ru, Rh, etc. are supported are used. As the porous carrier, alumina, silica, titania, alumina silica, alumina titania, alumina zirconia, silica magnesia, etc. are used. In particular, Ni-No%Co-Mo, Ni-Co-No, N1-V supported on alumina
It is preferable to use a catalyst such as
この第１段階の水素化処理は、石油蒸留物中のイオウ分
の除去を目的とするもので、石油蒸留物中のイオウ分が
０．４重量算以下、特に、０．２重量２以下になるよう
に行う０本発明では、このイオウ分の除去は、高い水素
化処理温度を採用したことにより効率よく行うことがで
きる。しかし、この第１段階の水素化処理では、得られ
る処理油は、その色相が、セイボルトカラー値で、通常
、−１０以下と悪化されたものである。この第１段階の
水素化処理生成物は、必要に応じ、ストリッピング処理
した後、第２段階の水素化処理に付される。The purpose of this first stage hydrogenation treatment is to remove the sulfur content in the petroleum distillate. According to the present invention, this sulfur content can be efficiently removed by employing a high hydrogenation temperature. However, in this first stage hydrogenation treatment, the treated oil obtained has a deteriorated hue, usually having a Saybolt color value of -10 or less. The first-stage hydrogenation product is subjected to a second-stage hydrogenation treatment after being subjected to a stripping treatment, if necessary.
（第２段階）
第２段階の水素化処理温度は、第１段階の水素化処理温
度よりも低められた温度であり１通常、１５０〜３２５
℃、好ましくは２００〜３００℃であり、圧力は５〜４
０ｋｇ／ｃｍ２、好ましくは１０−３０ｋｇ／ｃｍ２で
ある。液空間速度（Ｌ）ＩＳＶ）は０．５〜５．０ｈｒ
−’、好ましくは２．０−４．０ｈｒ−’であり、水素
ガス／原料油比率は５Ｏ−４５０ｒｒｉ’／ｋＱ。(Second stage) The hydrogenation temperature in the second stage is lower than the hydrogenation temperature in the first stage, and is usually 150 to 325%.
℃, preferably 200-300℃, and the pressure is 5-4
0 kg/cm2, preferably 10-30 kg/cm2. Liquid hourly space velocity (L) ISV) is 0.5 to 5.0 hr
-', preferably 2.0-4.0hr-', and the hydrogen gas/raw oil ratio is 5O-450rri'/kQ.
好ましくは８Ｇ−１６Ｏｎ？／ｋｆｉである。水素化処
理触媒としては、前記した如きの従来公知のものが用い
られる。Preferably 8G-16On? /kfi. As the hydrotreating catalyst, conventionally known catalysts as described above can be used.
第２段階の水素化処理は、第１段階の水素化処理により
得られる十分に低イオウ化されたものではあるが、逆に
色相が悪化した処理油の色相改善を目的とするもので、
生成処理油のセイボルトカラー値が０以上、好ましくは
５以上になるように行う。The second stage of hydrogenation treatment aims to improve the hue of the treated oil, which was obtained by the first stage of hydrogenation treatment and had a sufficiently low sulfur content, but whose hue had deteriorated.
The treatment is carried out so that the Saybolt color value of the resulting treated oil is 0 or more, preferably 5 or more.
色相悪化物質は、原料油中に含まれず、第１段階の水素
化処理により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。第２段階の水素化処理により色相
の改善が達成される理由は。The hue-deteriorating substance is not contained in the raw oil, but is newly generated by the first-stage hydrogenation treatment, and is considered to be a polycondensate of aromatic compounds. What is the reason why the second stage hydrogenation treatment improves the hue?
この芳香族化合物の重縮合体が核水素化され、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。This is thought to be due to the fact that this polycondensate of aromatic compounds undergoes nuclear hydrogenation and is converted into a hue-stable hydride without coloring.
第２段階の水素化処理で得られた生成物は、これを気液
分離した後、得られた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として回収され
る。このストリッピングにより分離される軽質留分は、
主に、第１段階の水素化処理により生成されたものであ
る。The product obtained in the second stage of hydrotreating is separated into gas and liquid, and then the resulting treated oil is stripped and the light fraction contained therein is separated and recovered as a product. Ru. The light fraction separated by this stripping is
It is mainly produced by the first stage of hydrogenation treatment.
本発明において、ｙＸ料油として、低イオウ分のものと
高イオウ分の２種を用いる場合、低イオウ分の原料油の
一部又は全部を第１段階の水素化生成物に混合して第２
段階の水素化処理を行うことにより、高温で実施される
第１段階の水素化処理の負担を軽減させることができる
。In the present invention, when two types of yX feedstock oils, one with a low sulfur content and the other with a high sulfur content, are used, part or all of the low sulfur content feedstock is mixed with the hydrogenated product in the first stage. 2
By performing the hydrogenation treatment in stages, it is possible to reduce the burden of the first stage hydrogenation treatment carried out at a high temperature.
次に１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。Next, a preferred embodiment of the present invention will be described with reference to the drawings.
第１図は本発明の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。第１図において、ｌ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。FIG. 1 shows a flow sheet for one preferred embodiment of the invention. In FIG. 1, 1 and 2 are reactors, 3 is a heating furnace, 5 is a heat exchanger, and 6 is a gas-liquid separator.
第１図において、Ｉ！Ｘ料油はライン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ｌに導入され、第１段階の水素
化処理を受ける。In Figure 1, I! The X feed oil passes through line 8 and pump 4, and further passes through heat exchanger 5, and is introduced into heating furnace 3 together with hydrogen gas from line 9, where it is heated to a predetermined temperature and then transferred to first reactor l. and undergoes the first stage of hydrogenation treatment.
反応器ｌからライン１４を通って抜出された処理油と水
素ガスとの混合物は、熱交換器５を通り、ここで原料油
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、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、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、製品としてライン
１３を通って回収される。The mixture of treated oil and hydrogen gas extracted from the reactor l through the line 14 passes through the heat exchanger 5, where it is heat exchanged with the feedstock oil and cooled to a predetermined temperature. , is introduced into the second reactor 2 and subjected to the second stage of hydrogenation treatment. The mixture of treated 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 separated into gas and liquid, and the separated gas components are passed through the line 15 as an off-gas. is discharged through the The treated oil, on the other hand, is introduced through line 11 to stripper 7, where the light fractions are separated through line 12 and recovered as product through line 13.
第２図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。FIG. 2 shows a flow sheet for another preferred embodiment of the invention.
第２図において、原料油はライン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ｌに導入
され、第１段階の水素化処理を受ける。In FIG. 2, feedstock oil is introduced into a heating furnace 3 through a line 8 and a pump 4 together with hydrogen gas from a line 9, heated there to a predetermined temperature, and then introduced into a first reactor l. It undergoes one stage of hydrotreating.
反応器１からライン１４を通って抜出された処理油と水
素ガスとの混合物は、循環ライン２１を通って循環され
る第２段階の水素化処理油と混合され。The mixture of treated oil and hydrogen gas withdrawn from the reactor 1 through line 14 is mixed with the second stage hydrotreated oil which is circulated through circulation line 21.
さらにライン２０からの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、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
通って抜出された処理油と水素ガスとの混合物は、第１
図に示した場合と同様にして後処理される。Furthermore, after being mixed with hydrogen gas from line 20 and cooled to a predetermined temperature, it is introduced into second reactor 2 and subjected to a second stage of hydrogenation treatment. The mixture of treated oil and hydrogen gas withdrawn from the second reactor through line 15 is transferred to the first reactor.
Post-processing is performed in the same manner as in the case shown in the figure.
（発明の効果）
本発明によれば、原料油をその色相を悪化させることな
く、効果的に低イオウ化させることができる０本発明の
方法は、低イオウ分であることが要求される自動車用軽
油の生産プロセスとして有利に適用される。(Effects of the Invention) According to the present invention, the method of the present invention can effectively reduce the sulfur content of feedstock oil without deteriorating its hue. It is advantageously applied as a production process of light oil for use.
（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。(Example) Next, the present invention will be explained in more detail with reference to Examples.
実施例
原料油として、直留軽油９０重量算と分解軽油１０重量
２との混合油を用いた。この混合油の比重（１５７４℃
）は０．８５３であり、イオウ分を１．０６重量算含有
するものであった。また、この混合油の蒸留開始点は２
０２℃であり、蒸留終点は３６２℃であった。As the raw material oil for the examples, a mixed oil of 90 parts by weight of straight-run gas oil and 10 parts by weight of cracked gas oil was used. Specific gravity of this mixed oil (1574℃
) was 0.853, and contained 1.06 sulfur by weight. Also, the starting point of distillation of this mixed oil is 2
The distillation end point was 362°C.
前記原料油を第１図に示したフローに°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。The raw material oil was subjected to two-stage hydrogenation treatment according to the flow shown in FIG. Table 1 shows the processing conditions and processing results.
Shown below.
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。For comparison, Table 1 also shows the results of treating the feedstock oil by one-step hydrotreating.
表−１
“・・・単位触媒容積に対する原料油の流量比（ｈｒ−
’ ）表−１に示した実験結果かられかるように、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１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＜、シ
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
。Table-1 “...Flow rate ratio of feedstock oil to unit catalyst volume (hr-
) As can be seen from the experimental results shown in Table 1, in Examples 1 and 2 according to the present invention, the sulfur content of the finally obtained treated oil is low and the hue is good. On the other hand, in Comparative Example 1, in order to obtain a low-sulfur treated oil at the same level as Examples 1 and 2, it is necessary to significantly reduce the amount of oil per pass, so the processing effect per hour of raw oil is poor. In Comparative Example 2, the reaction temperature was raised and the amount of oil passed was the same as in Examples 1 and 2 to obtain a low-sulfur treated oil. , in this case.
得られる処理油の色相は非常に悪いものとなる。The resulting treated oil has a very poor hue.
第１図は本発明の１つの実施態様についてのフローシー
トを示す、第２図は本発明の他の実施態様についてのブ
ローシートを示す。
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FIG. 1 shows a flow sheet for one embodiment of the invention, and FIG. 2 shows a blow sheet for another embodiment of the invention. 1.2... Reactor, 3... Heating furnace, 5... Heat exchanger, 6... Gas-liquid separator, 7... Stripper
Claims (1)
を水素化処理触媒の存在下で２段階で水素化処理するこ
とからなり、第１段階の水素化処理を温度２８０〜３７
０℃、圧力１０〜４０ｋｇ／ｃｍ＾２の条件下でイオウ
分が０．４重量％以下になるように行ない、第２段の水
素化処理を第１段階の水素化処理温度よりも低く、温度
１５０〜３２５℃、圧力１０〜４０ｋｇ／ｃｍ＾２の条
件下でセイボルトカラー値が０以上になるように行うこ
とを特徴とする石油蒸留物の低イオウ化方法。(1) The petroleum distillate containing 0.8 to 1.2% by weight of sulfur is hydrotreated in two stages in the presence of a hydrotreating catalyst, and the first stage of hydrogenation is carried out at a temperature of 280 to 280%. 37
The second stage hydrogenation treatment is carried out under conditions of 0°C and a pressure of 10 to 40 kg/cm^2 so that the sulfur content is 0.4% by weight or less, and the second stage hydrogenation temperature is lower than the first stage hydrogenation temperature. A method for reducing the sulfur content of a petroleum distillate, characterized in that the process is carried out under conditions of a temperature of 150 to 325°C and a pressure of 10 to 40 kg/cm^2 so that the Saybolt color value becomes 0 or more.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1223078A JP2530498B2 (en) | 1989-08-31 | 1989-08-31 | Method for reducing sulfur in petroleum distillates |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1223078A JP2530498B2 (en) | 1989-08-31 | 1989-08-31 | Method for reducing sulfur in petroleum distillates |
Related Child Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP31121993A Division JPH07102267A (en) | 1993-11-17 | 1993-11-17 | Method for improving hue of hydrotreated oil |
| JP31121893A Division JPH07102266A (en) | 1993-11-17 | 1993-11-17 | Method for reducing sulfur in petroleum distillates |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0386793A true JPH0386793A (en) | 1991-04-11 |
| JP2530498B2 JP2530498B2 (en) | 1996-09-04 |
Family
ID=16792496
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1223078A Expired - Lifetime JP2530498B2 (en) | 1989-08-31 | 1989-08-31 | Method for reducing sulfur in petroleum distillates |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2530498B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03292396A (en) * | 1990-04-10 | 1991-12-24 | Catalysts & Chem Ind Co Ltd | Method of hydrotreating kerosine or gas oil |
| US5403470A (en) * | 1993-01-28 | 1995-04-04 | Union Oil Company Of California | Color removal with post-hydrotreating |
| JPH07102267A (en) * | 1993-11-17 | 1995-04-18 | Tonen Corp | Method for improving hue of hydrotreated oil |
| US5888379A (en) * | 1995-08-21 | 1999-03-30 | Nippon Oil Co., Ltd. | Process for producing a fuel oil base material |
| WO2000026325A1 (en) * | 1998-10-30 | 2000-05-11 | Jgc Corporation | Gas turbine fuel oil and production method thereof and power generation method |
| US6454934B2 (en) | 1997-09-11 | 2002-09-24 | Jgc Corporation | Petroleum processing method |
| JP2003531274A (en) * | 2000-04-20 | 2003-10-21 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | Production of low sulfur distillate |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101245470B1 (en) | 2005-02-25 | 2013-03-25 | 에스케이에너지 주식회사 | Method for Preparation of Ultra Low Sulfur Diesel Fuel Having Improved Color Properties |
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| JPH0625677A (en) * | 1991-07-19 | 1994-02-01 | Nippon Oil Co Ltd | Production of low-sulfur diesel gas oil |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2793986A (en) * | 1952-11-25 | 1957-05-28 | Phillips Petroleum Co | Process and catalyst for hydrogenation of kerosene to remove color and fluorescence |
| GB934907A (en) * | 1961-07-31 | 1963-08-21 | Exxon Research Engineering Co | Improvements in the hydrofining of hydrocarbon liquids |
| US3392112A (en) * | 1965-03-11 | 1968-07-09 | Gulf Research Development Co | Two stage process for sulfur and aromatic removal |
| US3340183A (en) * | 1965-08-05 | 1967-09-05 | Chevron Res | Process for decolorizing oils |
| DE1545423A1 (en) * | 1966-08-16 | 1970-01-22 | Leuna Werke Veb | Process for the extensive removal of sulfur and olefins from hydrocarbon fractions boiling up to a maximum of 400 degrees Celsius |
| US3841995A (en) * | 1971-09-24 | 1974-10-15 | Standard Oil Co | Two-zone hydrogenation process for the production of colorless mineral oil |
| GB1476428A (en) * | 1973-07-03 | 1977-06-16 | Shell Int Research | Process for preparing white oils |
| JPS5310082A (en) * | 1976-07-14 | 1978-01-30 | Sumitomo Electric Ind Ltd | Connector detecting mechanism for core connecting machine |
| US4166026A (en) * | 1977-07-15 | 1979-08-28 | Chiyoda Chemical Engineering & Construction Co., Ltd. | Two-step hydrodesulfurization of heavy hydrocarbon oil |
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| JPH0539492A (en) * | 1991-08-07 | 1993-02-19 | Nippon Oil Co Ltd | Production of low sulfur diesel gas oil |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03292396A (en) * | 1990-04-10 | 1991-12-24 | Catalysts & Chem Ind Co Ltd | Method of hydrotreating kerosine or gas oil |
| US5403470A (en) * | 1993-01-28 | 1995-04-04 | Union Oil Company Of California | Color removal with post-hydrotreating |
| JPH07102267A (en) * | 1993-11-17 | 1995-04-18 | Tonen Corp | Method for improving hue of hydrotreated oil |
| US5888379A (en) * | 1995-08-21 | 1999-03-30 | Nippon Oil Co., Ltd. | Process for producing a fuel oil base material |
| US6454934B2 (en) | 1997-09-11 | 2002-09-24 | Jgc Corporation | Petroleum processing method |
| WO2000026325A1 (en) * | 1998-10-30 | 2000-05-11 | Jgc Corporation | Gas turbine fuel oil and production method thereof and power generation method |
| US7276151B1 (en) | 1998-10-30 | 2007-10-02 | Jgc Corporation | Gas turbine fuel oil and production method thereof and power generation method |
| JP2003531274A (en) * | 2000-04-20 | 2003-10-21 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | Production of low sulfur distillate |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2530498B2 (en) | 1996-09-04 |
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