JP3825876B2 - A heavy oil composition with good storage stability, hue stability and oil permeability - Google Patents
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Description
【０００１】
【発明の属する技術分野】
本発明、Ａ重油組成物に関する。更に詳しくは、直脱軽油を一定割合混合することにより、かつ残油系の残留炭素基材を使用しないこと、及び４０以上のセタン指数を有することにより、内燃機関等の燃料に適した貯蔵安定性、色相安定性及び通油性の良好な、内燃機関用として好適なＡ重油組成物に関する。
【０００２】
【従来の技術】
Ａ重油は、ＪＩＳ Ｋ ２２０５の１種１号又は２号の規定に適合するディーゼルエンジン等の内燃機関用、ボイラーや各種炉等の燃焼機器用の燃料として適当な品質を有する鉱物油である。一般にＡ重油は、地方税法第七百条に定められる軽油引取税の課税対象外となる４項目（密度・分留性状・残留炭素分・引火点）のうち、残留炭素分の項目を適用させている。そのため通常Ａ重油は常圧蒸留装置より得られる直留灯油（又は脱硫処理した灯油）、直留軽質軽油（又は脱硫処理した軽質軽油）、直留重質軽油（又は脱硫処理した重質軽油）の直留系基材を主体として用い、これに流動接触分解装置及び／又は残渣流動接触分解装置より得られる軽質サイクル油、減圧蒸留装置より得られる減圧軽油を水素化脱硫した水素化脱硫減圧軽油、水素化分解装置より得られる水素化分解軽油、直接重油脱硫装置より得られる直脱軽油等を混合し、更に残留炭素付与用の常圧残油、直脱残油、減圧残油等を混合して１０％残油の残留炭素分が０．２重量％をこえるように製造される。
【０００３】
近年の燃料油の需要動向は白油化傾向にあり、重質油を分解し白油を増産するための分解装置（流動接触分解装置、残渣流動接触分解装置、直接重油脱硫装置、水素化分解装置等）は、より稼働率が高まることが予想される。
【０００４】
現在、分解装置で製造される軽油相当の留分（分解軽油）は、主としてＡ重油のブレンド基材として、常圧蒸留装置から得られる直留軽油又は灯油の代替材源として用いることで白油増産に寄与しており、白油増産の観点から、分解軽油のＡ重油へのより一層の混合比率増加が急務となっている。
【０００５】
しかしながら、分解軽油の中でも軽質サイクル油は、貯蔵安定性に乏しいため貯蔵中に、燃焼機器のフィルター及びバーナ・ノズル等の閉塞の一因となる夾雑物を生じ易いことが知られており、そのままでは貯蔵安定性及び通油性確保の観点から一定量以上の混合は困難であった。
【０００６】
更に、軽質サイクル油は貯蔵中に褐色化が進み易いことが知られており、製品の品質維持の観点からも色相の安定化が求められていた。又、Ａ重油で一般的に使用される残油系残炭基材を添加する場合、貯蔵安定性、色相安定性、通油性が著しく悪化するという欠点を有しており、この点も改善が必要である。
【０００７】
軽質サイクル油は貯蔵安定性、色相安定性及び通油性を改善するために、これらに悪影響を与えると考えられているジエンやオレフィン化合物を飽和させ、反応性の高い硫黄化合物や窒素化合物を分解し、反応性の低い炭化水素、硫化水素、アンモニアを生成させるために水素化処理を行うのが効果的であるが、処理工程が増加し、コストがかかることから望ましいことではなかった。
【０００８】
又、軽質サイクル油の貯蔵安定性、色相安定性及び通油性改善のためには、上記の他に、苛性ソーダ洗浄によるチオフェノール、メルカプタン、硫化水素、有機酸、フェノール等の夾雑物前駆体除去や、安定化剤、酸化防止剤、分散剤、夾雑物生成反応を触媒する金属（特に銅）を不活性化する金属不活性化剤等の添加剤を添加する方法も存在するが、いずれもコスト増につながるものであった。
【０００９】
【発明が解決しようとする課題】
一般に、軽質サイクル油の貯蔵安定性、色相安定性及び通油性改善には水素化処理が最も効果的であるものの、処理工程が増加することから精製コストに大きく影響する。更に、水素化処理装置の処理能力の点からも容易に採用できない状況にある。
【００１０】
本発明の目的は、直脱軽油を一定割合以上混合することにより、特別な処理を施さずに軽質サイクル油を基材として可成り多量に使用しながら、貯蔵安定性、色相安定性及び通油性に優れ、内燃機関等の燃料に適したＡ重油組成物を提供することにある。
【００１１】
【課題を解決するための手段】
本発明者らは、従来のＡ重油組成物において、軽質サイクル油の混合による貯蔵安定性、色相安定性及び通油性の上記欠点を克服し、軽質サイクル油の水素化処理が不要なＡ重油組成物を開発すべく鋭意研究を重ねた結果、直脱軽油を軽質サイクル油に対し一定割合混合することにより、可成り多量に軽質サイクル油を使用しても貯蔵安定性、色相安定性及び通油性を改善する効果を見出し、本発明を完成するに至った。
【００１２】
すなわち、本発明の上記課題は、
１．（Ａ）沸点範囲１７０〜３８０℃、５０％留出点２００〜３３０℃、１５℃密度０．９００〜０．９８５ｇ／ｃｍ３の軽質サイクル油を４０容量％以上６０容量％未満と、
（Ｂ）沸点範囲１３０〜５００℃、５０％留出点２５０〜４００℃、１５℃密度０．８６０〜０．９５０ｇ／ｃｍ３の直脱軽油を７〜３０容量％と、
（Ｃ）その他の灯油又は軽油を含有し、
（Ｄ）かつ密度（１５℃）が０．８７６２ｇ／ｃｍ３をこえ、
（Ｅ）更に４０以上のセタン指数を有することを特徴とするＡ重油組成物、
２．（Ｃ）その他の灯油又は軽油が、（ａ）直留灯油又は脱硫処理した灯油、（ｂ）直留軽質軽油又は脱硫処理した軽質軽油、（ｃ）直留重質軽油又は脱硫処理した重質軽油、（ｄ）水素化分解軽油、及び（ｅ）水素化脱硫した減圧軽油のうちから選ばれる少なくとも１つであることを特徴とする前記１記載のＡ重油組成物、
３．直脱軽油が、沸点範囲１３０〜３３０℃、５０％留出点２００〜３００℃、１５℃密度０．８５０〜０．９００ｇ／ｃｍ３の直脱軽油中の低沸点留分であることを特徴とする前記１又は２記載のＡ重油組成物、
４．直脱軽油が、沸点範囲２２０〜４５０℃、５０％留出点２５０〜３５０℃、１５℃密度０．８６０〜０．９２０ｇ／ｃｍ３の直脱軽油中の中沸点留分であることを特徴とする前記１又は２記載のＡ重油組成物、
５．直脱軽油が、直脱軽油中の低沸点留分と中沸点留分を任意の割合で混合したものであることを特徴とする前記１又は２記載のＡ重油組成物、
６．軽質サイクル油が、流動接触分解装置及び／又は残渣流動接触分解装置より得られたものであり、直脱軽油が、直接重油脱硫装置より得られたものであることを特徴とする前記１〜５のいずれかに記載のＡ重油組成物、
の各々により達成される。
【００１３】
【発明の実施の形態】
以下に、本発明を更に詳細に説明する。本発明のＡ重油は所定の性状を有する軽質サイクル油を４０容量％以上６０容量％未満、及び所定の性状を有する直脱軽油又は直脱軽油のうち低沸点留分及び／又は中沸点留分を７〜３０容量％、残りはその他の灯油又は軽油とする割合で混合し、かつ、この際に１５℃密度が０．８７６２ｇ／ｃｍ３をこえ、更に４０以上のセタン指数を有するようにする。
【００１４】
この際、その他の灯油又は軽油は、（ａ）直留灯油又は脱硫処理した灯油、（ｂ）直留軽質軽油又は脱硫処理した軽質軽油、（ｃ）直留重質軽油又は脱硫処理した重質軽油、（ｄ）水素化分解軽油、及び（ｅ）水素化脱硫した減圧軽油のうちから選ばれる少なくとも１つであることが好ましい。
【００１５】
軽質サイクル油は、流動接触分解装置及び／又は残渣流動接触分解装置から得られる、沸点１７０〜３８０℃範囲内の留分である。具体的には、その蒸留性状として、５０％留出点が２００〜３３０℃であり、１５℃の密度が０．９００〜０．９８５ｇ／ｃｍ３の範囲のものが適宜利用できる。流動接触分解装置は、重質軽油、減圧軽油を水素化脱硫装置を用いて、アルミナ担持Ｃｏ−Ｍｏ触媒、アルミナ担持Ｎｉ−Ｍｏ触媒等の触媒存在下で、５〜１０ＭＰ、好ましくは５〜８ＭＰの圧力下、３５０〜４５０℃、好ましくは３６０〜４２０℃の温度で、ＬＨＳＶ ０．５〜４．０／ｈ、好ましくは１．０〜３．０／ｈの条件で水素化処理をした脱硫減圧軽油等を原料油に、又、残渣流動接触分解装置の場合は直接重油脱硫装置より得られる直脱残油、低硫黄の常圧残油を上記原料油に加えて、固体触媒の存在下で接触分解する装置であり、通常シリカアルミナ触媒やゼオライト触媒が用いられ、又、反応条件は一般に、反応温度４７０〜５５０℃、反応圧力０．０８〜０．３ＭＰ程度であるが、これらの条件は特に限定されるものではない。
【００１６】
直脱軽油は直接重油脱硫装置より得られる、沸点１３０〜５００℃の範囲内の留分である。具体的には、その蒸留性状として、５０％留出点が２５０〜４００℃であり、１５℃の密度が０．８６０〜０．９５０ｇ／ｃｍ３の範囲のものが適宜利用できる。直脱軽油のうち低沸点留分は、直接重油脱硫装置より得られる、沸点１３０〜３３０℃の範囲内の留分である。具体的には、その蒸留性状として、５０％留出点が２００〜３００℃であり、１５℃の密度が０．８５０〜０．９００ｇ／ｃｍ３の範囲のものが適宜利用できる。直脱軽油のうち中沸点留分は、直接重油脱硫装置より得られる、沸点２２０〜４５０℃の範囲内の留分である。具体的には、その蒸留性状として、５０％留出点が２５０〜３５０℃であり、１５℃の密度が０．８６０〜０．９２０ｇ／ｃｍ３の範囲のものが適宜利用できる。又、直接重油脱硫装置は、常圧残油及び／又は減圧残油をアルミナ担持Ｃｏ−Ｍｏ触媒、アルミナ担持Ｎｉ−Ｍｏ触媒等の触媒存在下で、１０〜２５ＭＰ、好ましくは１４〜２０ＭＰの圧力下、３５０〜４５０℃、好ましくは３６０〜４２０℃の温度で、ＬＨＳＶ ０．１〜１．０／ｈ、好ましくは０．２〜０．５／ｈの条件で水素化を行う装置であるが、これらの条件は特に限定されるものではない。
【００１７】
軽質サイクル油の混合割合が６０容量％以上の場合、４０以上のセタン指数を維持することが困難である。また、直脱軽油の混合割合が７容量％未満の場合は、直脱軽油による改質効果が不足して貯蔵安定性、色相安定性及び通油性の大きな改善効果は得られない。軽質サイクル油の混合割合が４０容量％未満の場合、及び／又は直脱軽油の混合割合が３０容量％をこえる場合は、１５℃密度を０．８７６２をこえることが困難であり、又コスト的に不利となり実際的ではなく、更に残炭基材の使用により軽油引取税の課税対象外とする場合は貯蔵安定性、色相安定性及び通油性が悪化する。
【００１８】
軽質サイクル油に対して直脱軽油を一定割合混合することにより貯蔵安定性、色相安定性、通油性が改善されることの理由は、必ずしも明確ではないが、原料油が直接重油脱硫装置で処理される過程で、多環芳香族等の一部が水素化され、反応性（水素供与能力）の高い化合物が生成し、これらの化合物が軽質サイクル油の反応性が高く不安定な化合物を安定化する作用を有するものと推定される。この効果は直留灯油（又は脱硫処理した灯油）、直留軽質軽油（又は脱硫処理した軽質軽油）、直留重質軽油（又は脱硫処理した重質軽油）、水素化分解軽油、及び水素化脱硫した減圧軽油にはなく、本発明で規定する直脱軽油を使用せずに、これらの直留系留分等だけを軽質サイクル油に混合した場合には貯蔵安定性、色相安定性及び通油性は改善されなかった。
【００１９】
本発明のＡ重油には、必要に応じてセタン価向上剤、酸化防止剤、安定化剤、分散剤、流動性向上剤、金属不活性化剤、微生物殺菌剤、助燃剤、帯電防止剤、識別剤等の各種添加剤を適宜加えることができる。
【００２０】
【実施例】
以下に実施例により本発明を詳細に説明するが、本発明はこれに限定されるものではない。
【００２１】
実施例１，２，３，４，５及び比較例１，２，３
表１に示す性状の基材を表２に示す容量比に混合して燃料組成物を調製し、その貯蔵安定性の指標として貯蔵前後のスラッジ重量の変化を、色相安定性の指標として貯蔵前後のＡＳＴＭ色の変化を、通油性の指標として貯蔵前後のフィルター通過時間を測定した。
【００２２】
【表１】
【表２】
表２より明らかなように、一定割合の直脱軽油又は直脱軽油のうち低沸点留分及び／又は中沸点留分を混合することにより、軽質サイクル油を可成り多量に混合してもスラッジ生成量を著しく低減し、優れた貯蔵安定性、色相安定性及び通油性を有するＡ重油が得られた。
【００２５】
尚、燃料油の性状及び貯蔵安定性は次の方法によって求めた。
【００２６】
＊１ 密度 ：ＪＩＳ Ｋ ２２４９に準拠して測定した。
【００２７】
＊２ 蒸留性状 ：ＪＩＳ Ｋ ２２５４に準拠して測定した。
【００２８】
＊３ スラッジ重量：スクリューキャップ付きのパイレックス製ビン（Ｃｏｒｎｉｎｇｌ３７２）のキャップに６ｍｍの穴を開け、試料充填後暗所にて８０℃で１週間貯蔵後、１００ｍｌを目開き０．８μｍのフィルターでろ過し、乾燥後ろ紙上に捕捉されたスラッジ重量を測定した。
【００２９】
＊４ ＡＳＴＭ色 ：ＪＩＳ Ｋ ２５８０に準拠して測定した。
【００３０】
＊５ 通油性 ：温度２０℃、吸引圧力５００ｍｍＨｇで、試料１０００ｍｌが直径４７ｍｍ、目開き０．８μｍのフィルターを通過するのに要する時間を測定した。
【００３１】
【発明の効果】
本発明によれば、一定割合の直脱軽油又は直脱軽油のうち低沸点留分及び／又は中沸点留分を混合することにより、軽質サイクル油を可成り多量に混合しても貯蔵安定性、色相安定性及び通油性の優れた、内燃機関等の燃料用として好適なＡ重油を製造することができ、軽質サイクル油の有効活用を図ることができる。[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a heavy oil composition A. More specifically, storage stability suitable for fuels of internal combustion engines, etc., by mixing a certain proportion of directly removed light oil, not using a residual oil base carbon base, and having a cetane index of 40 or more It is related with A heavy oil composition suitable for internal combustion engines with favorable property, hue stability, and oil permeability.
[0002]
[Prior art]
A heavy oil is a mineral oil having an appropriate quality as a fuel for an internal combustion engine such as a diesel engine or a combustion apparatus such as a boiler or various furnaces that conforms to JIS K 2205 No. 1 or No. 2. In general, for heavy fuel oil A, the residual carbon content item is applied among the 4 items (density, fractionation properties, residual carbon content, flash point) that are not subject to the taxation of diesel oil take-off tax stipulated in Article 700 of the Local Tax Law. ing. Therefore, A heavy oil is usually straight-run kerosene (or desulfurized kerosene), straight-run light diesel oil (or desulfurized light diesel oil), straight-run heavy diesel oil (or desulfurized heavy diesel oil) obtained from atmospheric distillation equipment. Hydrodesulfurized vacuum gas oil obtained by hydrodesulfurizing light cycle oil obtained from a fluid catalytic cracking device and / or residue fluid catalytic cracking device, and vacuum gas oil obtained from a vacuum distillation device. , Hydrocracked light oil obtained from hydrocracking equipment, direct dehydrated light oil obtained from direct heavy oil desulfurization equipment, etc. are mixed, and atmospheric residual oil for directing residual carbon, direct dehydrated residual oil, vacuum residual oil, etc. are mixed. Thus, the residual carbon content of 10% residual oil exceeds 0.2% by weight.
[0003]
The trend of demand for fuel oil in recent years has been the trend toward white oil, cracking equipment for cracking heavy oil and increasing white oil production (fluid catalytic cracking equipment, residual fluid catalytic cracking equipment, direct heavy oil desulfurization equipment, hydrocracking Equipment, etc.) is expected to have higher availability.
[0004]
At present, the fraction corresponding to light oil (cracked light oil) produced by the cracking device is mainly used as a blend base of heavy oil A, and is used as an alternative material source for straight-run light oil or kerosene obtained from the atmospheric distillation device. Contributing to increased production, and from the viewpoint of increasing white oil production, there is an urgent need to further increase the mixing ratio of cracked gas oil to heavy oil A.
[0005]
However, light cycle oils among cracked light oils are poor in storage stability, and are known to easily generate contaminants that may cause clogging of combustion equipment filters and burner nozzles during storage. However, it was difficult to mix more than a certain amount from the viewpoint of ensuring storage stability and oil permeability.
[0006]
Furthermore, light cycle oils are known to be easily browned during storage, and there has been a demand for stabilization of hue from the viewpoint of maintaining product quality. In addition, when the residual oil base material generally used in heavy oil A is added, it has the disadvantage that storage stability, hue stability, and oil permeability are remarkably deteriorated. is necessary.
[0007]
In order to improve storage stability, hue stability and oil permeability, light cycle oils saturate diene and olefin compounds that are thought to adversely affect them, and decompose highly reactive sulfur and nitrogen compounds. However, it is effective to perform a hydrotreatment to generate low-reactivity hydrocarbons, hydrogen sulfide, and ammonia, but this is not desirable because of an increase in processing steps and cost.
[0008]
In addition to the above, in order to improve the storage stability, hue stability and oil permeability of light cycle oil, in addition to the above, removal of contaminant precursors such as thiophenol, mercaptan, hydrogen sulfide, organic acid, phenol, etc. by washing with caustic soda There are also methods for adding additives such as stabilizers, antioxidants, dispersants, metal deactivators that inactivate metals (especially copper) that catalyze the formation of impurities, but they all cost It led to an increase.
[0009]
[Problems to be solved by the invention]
In general, hydrotreating is the most effective for improving the storage stability, hue stability and oil permeability of light cycle oils, but the refining cost is greatly affected by the increase in processing steps. Furthermore, it is in a situation where it cannot be easily adopted from the viewpoint of the processing capacity of the hydrotreating apparatus.
[0010]
The object of the present invention is to store a light cycle oil as a base material without any special treatment by mixing a directly degassed light oil at a certain ratio or more, while maintaining storage stability, hue stability and oil permeability. It is in providing an A heavy oil composition that is excellent in fuel and suitable for fuels such as internal combustion engines.
[0011]
[Means for Solving the Problems]
The present inventors have overcome the above-mentioned drawbacks of storage stability, hue stability and oil permeability due to mixing of light cycle oils in the conventional heavy fuel oil compositions, and A heavy oil compositions that do not require hydrogenation treatment of light cycle oils. As a result of intensive research to develop products, by mixing a certain amount of directly degassed light oil with light cycle oil, storage stability, hue stability and oil permeability even if a large amount of light cycle oil is used As a result, the present invention has been completed.
[0012]
That is, the above-described problem of the present invention is as follows.
1. (A) 40% by volume or more and less than 60% by volume of light cycle oil having a boiling point range of 170 to 380 ° C., 50% distillation point 200 to 330 ° C., 15 ° C. density 0.900 to 0.985 g / cm 3 ,
(B) Boiling range 130-500 ° C, 50% distilling point 250-400 ° C, 15 ° C density 0.860-0.950 g / cm 3 direct degassing light oil 7-30% by volume,
(C) contains other kerosene or light oil,
(D) and the density (15 ° C.) exceeds 0.8762 g / cm 3 ,
(E) A heavy oil composition further having a cetane index of 40 or more,
2. (C) Other kerosene or light oil is (a) straight-run kerosene or desulfurized kerosene, (b) straight-run light light oil or desulfurized light light oil, (c) straight-run heavy light oil or desulfurized heavy A heavy oil composition according to 1 above, which is at least one selected from gas oil, (d) hydrocracked gas oil, and (e) hydrodesulfurized vacuum gas oil,
3. The directly degassed diesel oil is a low boiling fraction in a directly degassed gas oil having a boiling range of 130 to 330 ° C., a 50% distillation point of 200 to 300 ° C., and a density of 15 ° C. of 0.850 to 0.900 g / cm 3. A heavy oil composition according to the above 1 or 2,
4). The direct degassing light oil is a medium boiling fraction in direct deionized light oil having a boiling point range of 220 to 450 ° C., a 50% distillation point of 250 to 350 ° C., and a density of 15 ° C. of 0.860 to 0.920 g / cm 3. A heavy oil composition according to the above 1 or 2,
5). The A heavy oil composition as described in 1 or 2 above, wherein the directly degassed oil is a mixture of a low boiling fraction and a medium boiling fraction in the directly degassed oil at an arbitrary ratio,
6). 1 to 5 above, wherein the light cycle oil is obtained from a fluid catalytic cracking device and / or a residue fluid catalytic cracking device, and the direct degassing light oil is obtained from a direct heavy oil desulfurization device. A heavy oil composition according to any one of
Achieved by each.
[0013]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, the present invention will be described in more detail. A heavy oil of the present invention is a light cycle oil having a predetermined property of 40% by volume or more and less than 60% by volume, and a direct boiling gas oil or a direct boiling gas oil having a predetermined property, a low boiling fraction and / or a medium boiling fraction. Is mixed at a ratio of 7 to 30% by volume, the rest being other kerosene or light oil, and at this time, the 15 ° C. density exceeds 0.8762 g / cm 3 and further has a cetane index of 40 or more. .
[0014]
At this time, the other kerosene or light oil is (a) straight-run kerosene or desulfurized kerosene, (b) straight-run light light oil or desulfurized light light oil, (c) straight-run heavy light oil or desulfurized heavy It is preferably at least one selected from light oil, (d) hydrocracked light oil, and (e) hydrodesulfurized vacuum light oil.
[0015]
The light cycle oil is a fraction having a boiling point in the range of 170 to 380 ° C. obtained from a fluid catalytic cracker and / or a residue fluid catalytic cracker. Specifically, as the distillation properties, those having a 50% distillation point of 200 to 330 ° C. and a density of 15 ° C. in the range of 0.900 to 0.985 g / cm 3 can be used as appropriate. The fluid catalytic cracking apparatus uses heavy hydro oil or vacuum gas oil in the presence of a catalyst such as an alumina-supported Co-Mo catalyst or an alumina-supported Ni-Mo catalyst using a hydrodesulfurization apparatus, and 5-10 MP, preferably 5-8 MP. Under the pressure of 350 ° C., preferably 360 ° C. to 420 ° C., and desulfurized by hydrogenation under the conditions of LHSV 0.5 to 4.0 / h, preferably 1.0 to 3.0 / h In the presence of a solid catalyst, add vacuum gas oil, etc. to the feedstock, and in the case of a residue fluid catalytic cracking unit, add direct debris residue obtained from a direct heavy oil desulfurization unit or low-sulfur atmospheric residue to the above feedstock. In general, a silica-alumina catalyst or a zeolite catalyst is used, and the reaction conditions are generally a reaction temperature of 470 to 550 ° C. and a reaction pressure of about 0.08 to 0.3 MP. Is not particularly limited Absent.
[0016]
Direct deionized light oil is a fraction having a boiling point in the range of 130 to 500 ° C., obtained directly from heavy oil desulfurization equipment. Specifically, as the distillation properties, those having a 50% distillation point of 250 to 400 ° C. and a density of 15 ° C. in the range of 0.860 to 0.950 g / cm 3 can be used as appropriate. The low boiling point fraction of direct degassed diesel oil is a fraction having a boiling point in the range of 130 to 330 ° C. obtained from a direct heavy oil desulfurization apparatus. Specifically, as the distillation properties, those having a 50% distillation point of 200 to 300 ° C. and a density of 15 ° C. in the range of 0.850 to 0.900 g / cm 3 can be used as appropriate. Among direct degassing light oils, the middle boiling fraction is a fraction having a boiling point within a range of 220 to 450 ° C. obtained from a direct heavy oil desulfurization apparatus. Specifically, as the distillation properties, those having a 50% distillation point of 250 to 350 ° C. and a density of 15 ° C. in the range of 0.860 to 0.920 g / cm 3 can be used as appropriate. Further, the direct heavy oil desulfurization apparatus is a pressure of 10 to 25 MP, preferably 14 to 20 MP in the presence of a catalyst such as an alumina-supported Co-Mo catalyst and an alumina-supported Ni-Mo catalyst. Below, it is an apparatus for performing hydrogenation under the conditions of LHSV 0.1-1.0 / h, preferably 0.2-0.5 / h at a temperature of 350-450 ° C., preferably 360-420 ° C. These conditions are not particularly limited.
[0017]
When the mixing ratio of light cycle oil is 60% by volume or more, it is difficult to maintain a cetane index of 40 or more. In addition, when the mixing ratio of the directly degassed light oil is less than 7% by volume, the reforming effect by the directly degassed light oil is insufficient, and a large improvement effect in storage stability, hue stability and oil permeability cannot be obtained. When the mixing ratio of the light cycle oil is less than 40% by volume and / or when the mixing ratio of the direct degassing light oil exceeds 30% by volume, it is difficult to exceed the density at 15 ° C. of 0.8762 and it is costly. However, if the base material of the residual carbon is not used, the storage stability, hue stability and oil permeability will deteriorate.
[0018]
The reason why storage stability, hue stability, and oil permeability are improved by mixing a certain amount of direct deionized light oil with light cycle oil is not necessarily clear, but the raw oil is processed directly with heavy oil desulfurization equipment. In the process, some of the polycyclic aromatics are hydrogenated to produce compounds with high reactivity (hydrogen donating ability), and these compounds stabilize the unstable compounds with high reactivity of light cycle oil. It is presumed to have an effect of This effect includes straight-run kerosene (or desulfurized kerosene), straight-run light diesel (or desulfurized light diesel), straight-run heavy diesel (or desulfurized heavy diesel), hydrocracked diesel, and hydrogenation When not only desulfurized vacuum gas oil but directly degassing oil oil specified in the present invention is used and only these straight-run fractions are mixed with light cycle oil, storage stability, hue stability and Oiliness was not improved.
[0019]
In the heavy oil A of the present invention, a cetane number improver, an antioxidant, a stabilizer, a dispersant, a fluidity improver, a metal deactivator, a microbial disinfectant, a combustion aid, an antistatic agent, Various additives such as an identification agent can be appropriately added.
[0020]
【Example】
The present invention will be described in detail below with reference to examples, but the present invention is not limited thereto.
[0021]
Examples 1, 2, 3, 4, 5 and Comparative Examples 1, 2, 3
A base material having the properties shown in Table 1 was mixed in the volume ratio shown in Table 2 to prepare a fuel composition, and the change in sludge weight before and after storage as an index of storage stability, and before and after storage as an index of hue stability. The change in ASTM color was measured using the filter passage time before and after storage as an index of oil permeability.
[0022]
[Table 1]
[Table 2]
As can be seen from Table 2, sludge can be mixed even if a large amount of light cycle oil is mixed by mixing a low boiling fraction and / or a middle boiling fraction out of a certain proportion of direct removed diesel oil or direct removed diesel oil. The amount of production was remarkably reduced, and A heavy oil having excellent storage stability, hue stability and oil permeability was obtained.
[0025]
The properties and storage stability of the fuel oil were determined by the following method.
[0026]
* 1 Density: Measured according to JIS K 2249.
[0027]
* 2 Distillation property: Measured according to JIS K 2254.
[0028]
* 3 Sludge weight: A 6 mm hole was made in the cap of a Pyrex bottle (Corning 372) with a screw cap, and after storing the sample in the dark at 80 ° C. for 1 week, 100 ml was filtered through a filter with an opening of 0.8 μm. The weight of sludge trapped on the dry back paper was measured.
[0029]
* 4 ASTM color: Measured according to JIS K 2580.
[0030]
* 5 Oil permeability: The time required for 1000 ml of the sample to pass through a filter having a diameter of 47 mm and an aperture of 0.8 μm at a temperature of 20 ° C. and a suction pressure of 500 mmHg was measured.
[0031]
【The invention's effect】
According to the present invention, by mixing a low-boiling fraction and / or a middle-boiling fraction of a certain proportion of directly degassed light oil or directly degassed light oil, storage stability is maintained even if light cycle oil is mixed in a considerably large amount. In addition, it is possible to produce A heavy oil that is excellent in hue stability and oil permeability and suitable for fuel for internal combustion engines and the like, and can effectively utilize light cycle oil.
Claims (6)
（Ｂ）沸点範囲１３０〜５００℃、５０％留出点２５０〜４００℃、１５℃密度０．８６０〜０．９５０ｇ／ｃｍ３の直脱軽油を７〜３０容量％と、
（Ｃ）その他の灯油又は軽油を含有し、
（Ｄ）かつ密度（１５℃）が０．８７６２ｇ／ｃｍ３をこえ、
（Ｅ）更に４０以上のセタン指数を有することを特徴とするＡ重油組成物。(A) 40% by volume or more and less than 60% by volume of light cycle oil having a boiling point range of 170 to 380 ° C., 50% distillation point 200 to 330 ° C., 15 ° C. density 0.900 to 0.985 g / cm 3 ,
(B) Boiling range 130-500 ° C, 50% distilling point 250-400 ° C, 15 ° C density 0.860-0.950 g / cm 3 direct degassing light oil 7-30% by volume,
(C) contains other kerosene or light oil,
(D) and the density (15 ° C.) exceeds 0.8762 g / cm 3 ,
(E) A heavy oil composition further having a cetane index of 40 or more.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| JP12481697A JP3825876B2 (en) | 1997-04-28 | 1997-04-28 | A heavy oil composition with good storage stability, hue stability and oil permeability |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12481697A JP3825876B2 (en) | 1997-04-28 | 1997-04-28 | A heavy oil composition with good storage stability, hue stability and oil permeability |
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| Publication Number | Publication Date |
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| JPH10298566A JPH10298566A (en) | 1998-11-10 |
| JP3825876B2 true JP3825876B2 (en) | 2006-09-27 |
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| JP4700153B2 (en) * | 1999-07-26 | 2011-06-15 | 出光興産株式会社 | Fuel oil |
| JP4577925B2 (en) * | 1999-08-05 | 2010-11-10 | Ｊｘ日鉱日石エネルギー株式会社 | A heavy oil composition |
| JP4635243B2 (en) * | 2007-05-31 | 2011-02-23 | Ｊｘ日鉱日石エネルギー株式会社 | A heavy oil |
| JP5153289B2 (en) * | 2007-10-16 | 2013-02-27 | 昭和シェル石油株式会社 | A heavy oil composition |
| JP7163176B2 (en) * | 2018-12-26 | 2022-10-31 | 出光興産株式会社 | Fuel oil composition for internal combustion engine |
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