JPS6341960B2 - - Google Patents
Info
- Publication number
- JPS6341960B2 JPS6341960B2 JP13472582A JP13472582A JPS6341960B2 JP S6341960 B2 JPS6341960 B2 JP S6341960B2 JP 13472582 A JP13472582 A JP 13472582A JP 13472582 A JP13472582 A JP 13472582A JP S6341960 B2 JPS6341960 B2 JP S6341960B2
- Authority
- JP
- Japan
- Prior art keywords
- kerosene
- oil
- naphtha
- light oil
- fraction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000003921 oil Substances 0.000 claims description 28
- 239000003350 kerosene Substances 0.000 claims description 20
- 238000006477 desulfuration reaction Methods 0.000 claims description 16
- 230000023556 desulfurization Effects 0.000 claims description 16
- 239000000295 fuel oil Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 8
- 239000003054 catalyst Substances 0.000 claims description 7
- 238000004821 distillation Methods 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims 1
- 239000012535 impurity Substances 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- 239000011593 sulfur Substances 0.000 description 7
- 229910052717 sulfur Inorganic materials 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 229910017464 nitrogen compound Inorganic materials 0.000 description 4
- 150000002830 nitrogen compounds Chemical class 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 238000001833 catalytic reforming Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000010941 cobalt Substances 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 229910052750 molybdenum Inorganic materials 0.000 description 3
- 239000011733 molybdenum Substances 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- 239000010779 crude oil Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 231100000989 no adverse effect Toxicity 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
【発明の詳細な説明】
本発明は脱硫軽質油の処理方法に関し、詳しく
は脱硫軽質油を精製分離して灯油やナフサを得る
方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for treating desulfurized light oil, and more particularly to a method for refining and separating desulfurized light oil to obtain kerosene or naphtha.
近時、大気汚染防止の要請から重油中の硫黄分
を除去する方法が採用されている。この重油脱硫
処理によつて硫黄分の含有率が低い高品質の重油
が得られるが、同時にナフサおよび灯油留分を含
む軽質油留分が副生する。この軽質油留分は、こ
のままでは製品として直ちに使用することができ
ないため、通常はエチレン等の製造のための熱分
解原料に用いられている。 Recently, methods for removing sulfur from heavy oil have been adopted in response to requests for air pollution prevention. This heavy oil desulfurization process yields high-quality heavy oil with a low sulfur content, but at the same time light oil fractions including naphtha and kerosene fractions are produced as by-products. Since this light oil fraction cannot be used immediately as a product as it is, it is usually used as a pyrolysis raw material for producing ethylene and the like.
しかし、この軽質油留分は熱分解原料として使
用するよりも、自動車ガソリンや灯油製品の原料
とする方が望ましい。このような原料として利用
するためには、軽質油留分に含まれている不純物
の除去と各製品への分離のために多大の設備を必
要とする。したがつて、製品の付加価値を向上さ
せることはできるが、製造コストの上昇を招くと
いう難点がある。 However, it is more desirable to use this light oil fraction as a raw material for automobile gasoline or kerosene products than as a pyrolysis raw material. In order to use it as such a raw material, a large amount of equipment is required to remove impurities contained in the light oil fraction and separate it into each product. Therefore, although it is possible to improve the added value of the product, it has the disadvantage of increasing manufacturing costs.
本発明の目的はこのような問題点を解消して脱
硫軽質油の精製分離を簡便かつ安価に行なつて自
動車ガソリンや灯油等として利用する方法を提供
することである。 The object of the present invention is to solve these problems and provide a method for simply and inexpensively refining and separating desulfurized light oil for use as automobile gasoline, kerosene, etc.
本発明は、重油脱硫装置から得られる脱硫軽質
油留分を灯軽油脱硫触媒と接触反応させたのち、
蒸留を行ない灯油とナフサを得ることを特徴とす
る脱硫軽質油の処理方法である。 In the present invention, after catalytically reacting the desulfurized light oil fraction obtained from the heavy oil desulfurization equipment with a kerosene and diesel oil desulfurization catalyst,
This is a method for processing desulfurized light oil, which is characterized by distilling it to obtain kerosene and naphtha.
重油脱硫装置は、原油の常圧蒸留残渣油を接触
水素化反応により脱硫して硫黄分0.1重量％程度
の脱硫重油とするものであり、触媒としてシリ
カ、アルミナあるいはシリカ−アルミナ担体にコ
バルト、モリブデン、ニツケル等の酸化物を担持
したものが使用され、温度370〜430℃、圧力150
Kg／cm2前後の条件にて反応が行なわれる。 Heavy oil desulfurization equipment desulfurizes residual oil from atmospheric distillation of crude oil by catalytic hydrogenation reaction to produce desulfurized heavy oil with a sulfur content of approximately 0.1% by weight. Silica, alumina, or silica-alumina carriers are used as catalysts, and cobalt and molybdenum are used. , oxides such as nickel are used, and the temperature is 370 to 430℃ and the pressure is 150℃.
The reaction is carried out under conditions of around Kg/ cm2 .
この重油脱硫装置では製品として低硫黄重質油
のほか２〜10容量％程度の軽質油が得られる。こ
の脱硫軽質油は軽質ナフサ留分から灯油留分に至
る広い沸点範囲の炭化水素の混合物であり、窒素
化合物などの不純物含量が高く、また貯蔵安定性
に劣る。すなわち、この軽質油は沸点範囲が30〜
190℃の留分であり、不純物として窒素化合物10
〜50ppm程度を含有している。それ故、この軽質
油はこのままでは前記した熱分解原料のほかには
格別の使途がない。 This heavy oil desulfurization equipment produces low-sulfur heavy oil as well as light oil of approximately 2 to 10% by volume. This desulfurized light oil is a mixture of hydrocarbons with a wide boiling point range ranging from light naphtha fractions to kerosene fractions, has a high content of impurities such as nitrogen compounds, and has poor storage stability. In other words, this light oil has a boiling point range of 30~
It is a distillate at 190℃, and contains 10 nitrogen compounds as impurities.
Contains about ~50ppm. Therefore, as it is, this light oil has no particular use other than as a raw material for pyrolysis as described above.
本発明では、この軽質油留分を灯軽油脱硫反応
塔に導入して窒素化合物などの不純物の除去およ
び不飽和化合物の水素添加をしたのち、蒸留塔へ
供給して精留分離を行ない、塔底油として灯油
を、塔頂油としてナフサをそれぞれ得るものであ
る。灯軽油脱硫反応塔は一般に重油脱硫装置と近
接して設置することが多いので、既設の装置を利
用すれば設備費は不要となり、精製コストを著し
く低減することができる。 In the present invention, this light oil fraction is introduced into a kerosene and gas oil desulfurization reaction tower to remove impurities such as nitrogen compounds and hydrogenate unsaturated compounds, and then supplied to a distillation tower for rectification separation. Kerosene is obtained as the bottom oil and naphtha is obtained as the top oil. Kerosene and gas oil desulfurization reaction towers are generally installed in close proximity to heavy oil desulfurization equipment, so if existing equipment is used, equipment costs are unnecessary and refining costs can be significantly reduced.
灯軽油脱硫装置は原油の常圧蒸留により得られ
る灯油または軽油の脱硫に用いられるものであ
り、本発明においても前記軽質油留分を対象とし
て、シリカ、アルミナ、シリカ−アルミナ等の担
体にニツケル、コバルト、モリブデン、タングス
テン等の金属の酸化物を担持させたものを触媒と
して用い、温度310〜370℃、圧力20〜50Kg／cm2の
条件下で水素化脱硫を行なう。不純物を除いた留
分は常圧留塔に供給して精留を行なう。ここで塔
底油として得られる灯油は燃焼性、貯蔵安定性、
色相、臭気などいずれの性状においても優れてお
り、製品として使用することができる。一方、塔
頂油として得られるナフサはナフサ脱硫装置にお
いて軽質ナフサと重質ナフサに分離し、重質ナフ
サについてはさらに接触改質装置に導入して自動
車ガソリンとすることができる。この場合、ナフ
サ中の硫黄や窒素化合物など不純物の含有量が少
ないので、接触改質触媒に悪影響を及ぼすことが
ない。 Kerosene desulfurization equipment is used to desulfurize kerosene or gas oil obtained by atmospheric distillation of crude oil, and in the present invention, the light oil fraction is also treated with nickel on a carrier such as silica, alumina, or silica-alumina. Hydrodesulfurization is carried out at a temperature of 310 to 370° C. and a pressure of 20 to 50 kg/cm 2 using a supported oxide of a metal such as cobalt, molybdenum, or tungsten as a catalyst. The fraction from which impurities have been removed is supplied to an atmospheric distillation tower for rectification. The kerosene obtained as bottom oil here has good flammability, storage stability,
It has excellent properties such as color and odor, and can be used as a product. On the other hand, naphtha obtained as overhead oil is separated into light naphtha and heavy naphtha in a naphtha desulfurization device, and the heavy naphtha can be further introduced into a catalytic reforming device to produce automobile gasoline. In this case, since the content of impurities such as sulfur and nitrogen compounds in the naphtha is small, there is no adverse effect on the catalytic reforming catalyst.
本発明によれば、重油脱硫装置から得られる脱
硫軽質油留分の精製分離を簡便に、かつ低コスト
で実施することができる。しかも、本発明の方法
によつて得られる灯油は高品質のものであり、ま
た重質ナフサは不純物含量が少ないため、接触改
質触媒を被毒することなく有用な自動車ガソリン
に変換することができる。 According to the present invention, the refining and separation of the desulfurized light oil fraction obtained from the heavy oil desulfurization equipment can be carried out easily and at low cost. Moreover, the kerosene obtained by the method of the present invention is of high quality, and the heavy naphtha has a low impurity content, so it can be converted into useful automobile gasoline without poisoning the catalytic reforming catalyst. can.
次に、本発明を実施例により説明する。 Next, the present invention will be explained by examples.
実施例
原料として、重油脱硫装置から得られた脱硫軽
質油留分（沸点範囲30〜155℃）を水素の存在下
に温度350℃、圧力40気圧、LHSV2.5hr-1の条件
でコバルトとモリブデンの複合酸化物をアルミナ
に担持した灯軽油脱硫触媒と接触させ、得られた
反応生成物を常圧で蒸留分離した。Example As a raw material, a desulfurized light oil fraction (boiling point range 30 to 155°C) obtained from a heavy oil desulfurization equipment was processed into cobalt and molybdenum in the presence of hydrogen at a temperature of 350°C, a pressure of 40 atm, and a LHSV of 2.5 hr -1 . The composite oxide was brought into contact with a kerosene desulfurization catalyst supported on alumina, and the resulting reaction product was separated by distillation at normal pressure.
この結果、原料に対して45容量％の収率で灯油
留分が得られ、この灯油留分中の硫黄分は
10ppm、窒素分0.5ppmであり、高品質の灯油製
品であつた。残部はナフサ留分として回収され、
このナフサ留分中の硫黄分は5ppm、窒素分は
0.3ppmであり、ナフサ脱硫装置において処理し
たのち、白金触媒によるナフサ改質装置への供給
原料に使用できることが判明した。 As a result, a kerosene fraction was obtained with a yield of 45% by volume based on the raw material, and the sulfur content in this kerosene fraction was
It was a high quality kerosene product with a nitrogen content of 10ppm and 0.5ppm. The remainder is recovered as naphtha fraction,
The sulfur content in this naphtha fraction is 5ppm, and the nitrogen content is
0.3 ppm, and after treatment in a naphtha desulfurization unit, it was found that it could be used as a feedstock to a platinum-catalyzed naphtha reformer.
Claims (1)
灯軽油脱硫触媒と接触反応させたのち、蒸留を行
ない灯油とナフサを得ることを特徴とする脱硫軽
質油の処理方法。1. A method for processing desulfurized light oil, which comprises subjecting a desulfurized light oil fraction obtained from a heavy oil desulfurization equipment to a catalytic reaction with a kerosene and gas oil desulfurization catalyst, followed by distillation to obtain kerosene and naphtha.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13472582A JPS5925887A (en) | 1982-08-03 | 1982-08-03 | Method for treating desulfurized light oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13472582A JPS5925887A (en) | 1982-08-03 | 1982-08-03 | Method for treating desulfurized light oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5925887A JPS5925887A (en) | 1984-02-09 |
| JPS6341960B2 true JPS6341960B2 (en) | 1988-08-19 |
Family
ID=15135136
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP13472582A Granted JPS5925887A (en) | 1982-08-03 | 1982-08-03 | Method for treating desulfurized light oil |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5925887A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63259215A (en) * | 1987-04-13 | 1988-10-26 | Sanwa Niidorubearingu Kk | Thrust bearing device having fluid retaining groove and its manufacture |
| JPH0860165A (en) | 1994-08-24 | 1996-03-05 | Idemitsu Kosan Co Ltd | Fuel oil composition and production thereof |
-
1982
- 1982-08-03 JP JP13472582A patent/JPS5925887A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5925887A (en) | 1984-02-09 |
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