JP2007119648A - Method for treating plastic cracked oil - Google Patents

Method for treating plastic cracked oil Download PDF

Info

Publication number
JP2007119648A
JP2007119648A JP2005315547A JP2005315547A JP2007119648A JP 2007119648 A JP2007119648 A JP 2007119648A JP 2005315547 A JP2005315547 A JP 2005315547A JP 2005315547 A JP2005315547 A JP 2005315547A JP 2007119648 A JP2007119648 A JP 2007119648A
Authority
JP
Japan
Prior art keywords
oil
plastic
cracked oil
plastic cracked
crude oil
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.)
Granted
Application number
JP2005315547A
Other languages
Japanese (ja)
Other versions
JP4787598B2 (en
Inventor
Hiroaki Wakao
博明 若尾
Nobuyuki Shiratori
伸之 白鳥
Takasato Kasai
崇智 河西
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Eneos Corp
Original Assignee
Japan Energy Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Japan Energy Corp filed Critical Japan Energy Corp
Priority to JP2005315547A priority Critical patent/JP4787598B2/en
Publication of JP2007119648A publication Critical patent/JP2007119648A/en
Application granted granted Critical
Publication of JP4787598B2 publication Critical patent/JP4787598B2/en
Expired - Fee Related legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for producing a naphtha fraction and a kerosene gas oil fraction, which become a gasoline base raw material, a petrochemical raw material and a kerosene gas oil, as well as a heavy oil, by resolving a problem during treating a plastic cracked oil together with a component derived from a crude oil at a petroleum refining process. <P>SOLUTION: This method for treating the plastic cracked oil comprises treating a mixture of the plastic cracked oil produced by cracking plastic and a component derived from the crude oil at the petroleum refining process, wherein a 90% recovered temperature of the component derived from the crude oil is ≥a 90% recovered temperature of the plastic cracked oil. It is preferred that the 90% recovered temperature of the component derived from the crude oil is ≥200°C and/or the component derived from the crude oil is a residual oil. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

本発明は、プラスチックの分解によって生成するプラスチック分解油を石油精製工程において原油由来成分とともに処理し、ガソリン基材原料や石油化学原料及び灯軽油となるナフサ留分や灯軽油留分並びに重油などを製造する方法に関する。   The present invention treats plastic cracked oil produced by cracking plastic together with components derived from crude oil in the petroleum refining process to produce naphtha fraction, kerosene oil fraction, heavy oil, etc., which become gasoline base material, petrochemical raw material, and kerosene oil. It relates to a method of manufacturing.

一般に原油から製造されるガソリン基材原料や石油化学原料となるナフサ留分や灯油・軽油留分は需要が旺盛である。この原料としては、直留ナフサ、減圧ナフサ、熱分解ナフサ、直留灯油、減圧灯油、熱分解灯油、直留軽油、減圧軽油、熱分解軽油など原油から得られる石油留分が用いられている。   In general, there is a strong demand for naphtha fractions, kerosene and light oil fractions, which are gasoline base materials and petrochemical materials produced from crude oil. As this raw material, petroleum fractions obtained from crude oil such as straight-run naphtha, vacuum naphtha, pyrolysis naphtha, straight-run kerosene, vacuum kerosene, pyrolysis kerosene, straight-run gas oil, vacuum gas oil, and pyrolysis gas oil are used. .

プラスチック分解油は、廃棄物などから分離されたプラスチックの分解によって生成する油分である。原料となるプラスチックは、特に限定されるものではないが、ポリエチレン、ポリプロピレンなどのポリオレフィン、ポリスチレンなどのスチレン系樹脂、ポリアミド樹脂、ポリ塩化ビニル、ポリ塩化ビニリデン、ポリカーボネートなどが挙げられる。通常は、廃棄されたプラスチックを原料とする。このようなプラスチックの熱分解反応は公知である（特許文献１、２参照）。   Plastic cracked oil is an oil produced by cracking plastic separated from waste or the like. The raw material plastic is not particularly limited, and examples thereof include polyolefins such as polyethylene and polypropylene, styrene resins such as polystyrene, polyamide resins, polyvinyl chloride, polyvinylidene chloride, and polycarbonate. Usually, discarded plastic is used as a raw material. Such a thermal decomposition reaction of plastic is known (see Patent Documents 1 and 2).

このプラスチック分解油は、一般的にボイラー燃料などに用いられており、不純物が多いことからガソリン基材や灯軽油、石油化学原料として利用されていない。廃プラスチック中、ポリアミド樹脂、ポリウレタン類、ＡＢＳ樹脂及びＮＢＲには窒素が含有され、ポリ塩化ビニル（ＰＶＣ）、ポリ塩化ビニリデン（ＰＶＤＣ）、塩化ポリエチレンには塩素が含有される。このため、プラスチック分解油中には塩素分、窒素分 など不純物が比較的多く残存しており、これを除去するために、一度プラスチック分解油を単独で前処理（水素化精製）することによって脱塩素を行い、その後石油留分と混合して石油精製工程にて処理することが提案されている。（特許文献３，４，５参照）   This plastic cracked oil is generally used for boiler fuel and the like, and since it has many impurities, it is not used as a gasoline base material, kerosene oil, or petrochemical raw material. Among waste plastics, polyamide resins, polyurethanes, ABS resins, and NBR contain nitrogen, and polyvinyl chloride (PVC), polyvinylidene chloride (PVDC), and polyethylene chloride contain chlorine. For this reason, relatively large amounts of impurities such as chlorine and nitrogen remain in the cracked plastic oil, and in order to remove this, the plastic cracked oil is once removed by pretreatment (hydrorefining) alone. It has been proposed to perform chlorine, then mix with petroleum fractions and process in the oil refining process. (See Patent Documents 3, 4, and 5)

プラスチック分解油を単独で前処理（水素化精製）するためには、新しい設備が必要であり、運転コストも高い。このため、前処理をせず、石油留分と混合して石油精製工程にて処理することが提案されている。（特許文献６参照）   In order to pre-process (hydrorefining) the plastic cracked oil alone, new equipment is required and the operating cost is high. For this reason, it has been proposed to mix with an oil fraction and process in an oil refining process without pretreatment. (See Patent Document 6)

しかし、プラスチック分解油をそのままでは、実質的には水素化精製することができない。プラスチック分解油には不純物としてオレフィン分が多く含まれていることがある。オレフィン分は熱により重合し、処理装置に汚れが発生、触媒上にコーキングを起こし処理が困難となることがある。例えば、熱交換器においては、プラスチック分解油による汚れが内面に析出するために熱交換効率が悪化したり、触媒上にコーキングを起きるため通油が困難になり、所定の運転ができないことがある。   However, if the plastic cracked oil is used as it is, it cannot be substantially hydrorefined. Plastic cracked oil may contain a large amount of olefins as impurities. The olefin content is polymerized by heat, causing contamination in the processing apparatus, causing coking on the catalyst and making the processing difficult. For example, in a heat exchanger, dirt due to plastic decomposition oil is deposited on the inner surface, so heat exchange efficiency is deteriorated, or caulking occurs on the catalyst, making it difficult to pass oil, and a predetermined operation may not be performed. .

また、石油精製工程において、プラスチック分解油を原油と混合して常圧蒸留装置に入れて処理することが考えられるが、以下の問題があり困難である。プラスチック分解油の各留分には塩素分、窒素分などの不純物が多く、これらの不純物は原油には含まれない。プラスチック分解油を原油と混合して常圧蒸留装置で分留すると、各留分には塩素分、窒素分などの不純物が含まれることとなる。しかし、常圧蒸留装置からの留分のうち、軽質ナフサなどの多くの留分はそのまま、精製処理を経ることなく製品としている。このため、製品に従来含まれない塩素分、窒素分などの不純物が含まれることになる。さらに、プラスチック分解油由来のナフサ、特には重質ナフサを水素化精製しようとすると、汚れ起因物質、例えばスチレン、αメチルスチレンなどが重合を起こし、汚れ、閉塞を発生させ、安定的な長期運転ができない。
特開平０９−２３５５６３号公報 特開２００２−６０７５７号公報 特開平１１−０６１１４８号公報 特開平０９−０４８９８３号公報 特表平０８−５０８５２０号公報 特開２００５−１０５０２７号公報 In the oil refining process, it is conceivable that the plastic cracked oil is mixed with crude oil and placed in an atmospheric distillation apparatus, but this is difficult due to the following problems. Each fraction of plastic cracked oil has many impurities such as chlorine and nitrogen, and these impurities are not contained in crude oil. When plastic cracked oil is mixed with crude oil and fractionated with an atmospheric distillation device, impurities such as chlorine and nitrogen are contained in each fraction. However, among the fractions from the atmospheric distillation apparatus, many fractions such as light naphtha are used as products without undergoing purification treatment. For this reason, impurities such as chlorine and nitrogen that are not conventionally included in the product are included. Furthermore, when hydrotreating naphtha derived from plastic cracked oil, especially heavy naphtha, dirt-causing substances such as styrene and α-methyl styrene cause polymerization, causing dirt and clogging, and stable long-term operation. I can't.
JP 09-235563 A JP 2002-60757 A Japanese Patent Laid-Open No. 11-061148 JP 09-049883 A Japanese National Patent Publication No. 08-508520 JP 2005-105027 A

本発明はこのようなプラスチック分解油の石油精製工程における処理における問題点を解決し、プラスチック分解油をガソリン基材原料や石油化学原料及び灯軽油となるナフサ留分及び灯軽油留分、重油基材として利用することを目的とするものである。   The present invention solves the problems in the processing of such a plastic cracked oil in the oil refining process, and the plastic cracked oil is converted into gasoline base material, petrochemical raw material, kerosene oil, naphtha fraction, kerosene oil fraction, heavy oil base. It is intended to be used as a material.

本発明によるプラスチック分解油処理方法は、プラスチックの分解によって生成するプラスチック分解油を原油由来成分と混合し、石油精製工程において処理するプラスチック分解油処理方法であって、前記原油由来成分の９０％留出温度が、前記プラスチック分解油の９０％留出温度以上である。前記原油由来成分の９０％留出温度が、２００℃以上であること、及び／又は、前記原油由来成分が残さ油であることが好ましい。   The plastic cracking oil processing method according to the present invention is a plastic cracking oil processing method in which a plastic cracking oil produced by the decomposition of plastic is mixed with a crude oil-derived component and treated in a petroleum refining process. The exit temperature is equal to or higher than the 90% distillation temperature of the plastic cracked oil. The 90% distillation temperature of the crude oil-derived component is preferably 200 ° C. or higher, and / or the crude oil-derived component is a residual oil.

前記プラスチック分解油の１０％留出温度が２００℃未満であること、及び／又は、前記プラスチック分解油の初留点が１００℃未満であること、及び／又は、前記プラスチック分解油の９０％留出温度が３００℃を超え、６００℃以下であることが好ましい。   The 10% distillation temperature of the plastic cracked oil is less than 200 ° C, and / or the initial boiling point of the plastic cracked oil is less than 100 ° C, and / or 90% of the plastic cracked oil is distilled. It is preferable that the exit temperature is higher than 300 ° C and lower than 600 ° C.

前記石油精製工程は、水素化精製、水素化分解及び接触分解の少なくとも一つの工程を含むことが好ましい。   The petroleum refining step preferably includes at least one step of hydrorefining, hydrocracking, and catalytic cracking.

本発明は、特定の性状からなるプラスチック分解油を、特定の性状からなる原油由来成分と混合して、石油精製工程で処理するものであり、石油精製工程において、汚れ、コーキングなどの問題を生じることなく処理することが可能となり、特に、水素化精製処理により塩素分、窒素分など不純物を低減できる。したがって、不純物含有量の少ないプラスチック分解油を得ることができ、ガソリン基材原料や石油化学原料、灯軽油および重油基材として利用することができる。 In the present invention, a plastic cracked oil having a specific property is mixed with a crude oil-derived component having a specific property and processed in an oil refining process, which causes problems such as dirt and coking in the oil refining process. In particular, impurities such as chlorine and nitrogen can be reduced by hydrorefining treatment. Accordingly, it is possible to obtain a plastic cracked oil having a small impurity content, and it can be used as a gasoline base material, petrochemical raw material, kerosene oil, and heavy oil base material.

〔プラスチック分解油〕
プラスチック分解油は、プラスチックの分解によって得られたものであり、蒸留性状は１０％留出温度が２００℃未満であることが好ましく、特には、１８０℃以下、更には１５０℃以下が好ましい。初留点は１００℃以下、特には５０℃以下であることが好ましい。９０％留出温度が３００℃〜６００℃、特には、３５０℃を超える、更には４００℃を超えることが好ましい。プラスチックの分解方法としては、熱分解、接触分解、加水分解、アルコリシスなどの解重合などの方法があるが、熱分解による分解油が好ましい。 [Plastic decomposition oil]
The plastic cracked oil is obtained by decomposing plastic, and the distillation property is preferably 10% distillation temperature of less than 200 ° C., particularly preferably 180 ° C. or less, more preferably 150 ° C. or less. The initial boiling point is preferably 100 ° C. or lower, particularly 50 ° C. or lower. The 90% distillation temperature is preferably 300 ° C. to 600 ° C., more preferably 350 ° C., and even more preferably 400 ° C. As a method for decomposing plastics, there are methods such as depolymerization such as thermal decomposition, catalytic decomposition, hydrolysis, alcoholysis, and the like, but decomposition oil by thermal decomposition is preferable.

プラスチック分解油の性状としては、硫黄分が２００００ｐｐｍ以下、特には３００ｐｐｍ以下、窒素分が２０００ｐｐｍ以下、特には１５００ｐｐｍ以下、塩素分が１〜１０００ｐｐｍ、特には１０〜１００ｐｐｍ、臭素価が１．５ｇＢｒ２／１００ｇ以上、特には１０〜３００ｇＢｒ２／１００ｇ、ジエン価が０．３ｇ／１００ｇ以上、特には１〜５ｇ／１００ｇであることが好ましい。なお、不純物などがこの範囲を外れる場合には、吸着、ろ過、遠心分離などの除去処理により予めプラスチック分解油を処理して不純物を除去することもできる。また、残炭素分が０．０１〜１０重量％、特には０．１〜５重量％、アスファルテン分が０．０５〜５重量％、特には０．１〜３重量％であることが好ましい。 As the properties of the plastic cracked oil, the sulfur content is 20000 ppm or less, particularly 300 ppm or less, the nitrogen content is 2000 ppm or less, particularly 1500 ppm or less, the chlorine content is 1-1000 ppm, particularly 10-100 ppm, and the bromine number is 1.5 gBr 2. / 100g or more, particularly 10～300GBr 2 / 100g, diene value 0.3 g / 100g or more, and particularly preferably from 1 to 5 g / 100g. In addition, when an impurity etc. remove | deviates from this range, a plastic decomposition oil can be previously processed by removal processes, such as adsorption | suction, filtration, and centrifugation, and an impurity can also be removed. The residual carbon content is preferably 0.01 to 10% by weight, particularly 0.1 to 5% by weight, and the asphaltene content is preferably 0.05 to 5% by weight, and particularly preferably 0.1 to 3% by weight.

〔原油由来成分〕
原油由来成分の蒸留性状について、９０％留出温度は、プラスチック分解油の９０％留出温度以上、特には１００℃以上、さらには２００℃以上高いことが好ましい。また、９０％留出温度は、
２００℃以上、特には４００℃以上が好ましい。特には残さ油（直留残さ油、減圧残さ油）であることが好ましい。原油由来成分の芳香族分は、１０〜５０％、特には２０〜４０％が好ましい。原油由来成分の９０％留出温度がこの範囲であれば、原油由来成分中に多くの芳香族分を有し、溶解性が高いため、コーキングを抑制しながら処理できるため、好ましい。 [Crude oil-derived components]
Regarding the distillation properties of crude oil-derived components, the 90% distillation temperature is preferably higher than the 90% distillation temperature of the plastic cracked oil, particularly 100 ° C or higher, more preferably 200 ° C or higher. The 90% distillation temperature is
200 degreeC or more, Especially 400 degreeC or more is preferable. In particular, a residual oil (straight-run residual oil, reduced pressure residual oil) is preferable. The aromatic component of the crude oil-derived component is preferably 10 to 50%, particularly preferably 20 to 40%. If the 90% distillation temperature of the crude oil-derived component is within this range, it is preferable because the crude oil-derived component has a large amount of aromatic components and has high solubility, and can be treated while suppressing coking.

原油由来成分は、原油を原料として得られた炭化水素からなる成分であれば特に限定はなく、例えば、直留ナフサ、減圧ナフサ、熱分解ナフサ、直留灯油、減圧灯油、熱分解灯油、直留軽油、減圧軽油、熱分解軽油、直留残さ油、減圧残さ油などやこれらの任意な混合物が挙げられる。   The crude oil-derived component is not particularly limited as long as it is a component made of hydrocarbons obtained from crude oil. For example, straight-run naphtha, vacuum naphtha, pyrolysis naphtha, straight-run kerosene, vacuum kerosene, pyrolysis kerosene, straight Examples thereof include distillate oil, vacuum gas oil, pyrolysis gas oil, straight-run residue oil, vacuum residue oil, and any mixture thereof.

原油由来成分は、硫黄分が０．０５〜１０％、特には０．１〜５％、窒素分が１０〜５０００ｐｐｍ、特には２０〜２０００ｐｐｍであることが好ましい。また、残炭素分が１〜３０重量％、特には５〜２５重量％、アスファルテン分が１〜１０重量％、特には２〜５重量％であることが好ましい。   The crude oil-derived component preferably has a sulfur content of 0.05 to 10%, particularly 0.1 to 5%, and a nitrogen content of 10 to 5000 ppm, particularly 20 to 2000 ppm. The residual carbon content is preferably 1 to 30% by weight, particularly 5 to 25% by weight, and the asphaltene content is preferably 1 to 10% by weight, particularly 2 to 5% by weight.

プラスチック分解油の混合割合は、処理対象全体に対して５０容量％以下、特には２５容量％以下、さらには０．１〜２０容量％が好ましい。この範囲を超える場合にはコーキング及び／又は腐食が予想され、処理が困難になることが予想される。   The mixing ratio of the plastic cracked oil is preferably 50% by volume or less, particularly 25% by volume or less, more preferably 0.1 to 20% by volume with respect to the entire processing target. If this range is exceeded, coking and / or corrosion is expected and processing is expected to be difficult.

〔石油精製工程〕
プラスチック分解油と原油由来成分を混合した混合原料油を処理する石油精製工程は、水素化精製、水素化分解および接触分解の少なくとも一つの工程を含むものであり、特に、水素化精製の工程が好ましい。これにより、原油由来成分の硫黄分、窒素分、金属分などが低減されるとともに、プラスチック分解油の窒素分、塩素分、金属分などが低減される。硫黄分が０．５〜５％、特には１％以上の石油留分をプラスチック分解油と混合して、水素化精製により硫黄分が１％以下、特には０．５％以下とするような精製工程が好ましい。 [Oil refinery process]
The oil refining process for processing mixed feedstock mixed with plastic cracked oil and crude oil-derived components includes at least one process of hydrorefining, hydrocracking and catalytic cracking. preferable. Thereby, the sulfur content, nitrogen content, metal content, etc. of the crude oil-derived component are reduced, and the nitrogen content, chlorine content, metal content, etc. of the plastic decomposition oil are reduced. A petroleum fraction having a sulfur content of 0.5 to 5%, particularly 1% or more is mixed with plastic cracked oil, and the sulfur content is reduced to 1% or less, particularly 0.5% or less by hydrorefining. A purification step is preferred.

水素化精製は処理油を水素の存在下で水素化精製触媒と接触させるものである。水素化精製触媒は、アルミナなどの無機多孔質担体にモリブデン、ニッケル、コバルト、リンのうち少なくとも一種を、特にモリブデンとニッケルまたはコバルトの少なくとも一方を担持した触媒が好ましく用いられる。好ましい反応条件は反応温度：２５０〜４５０℃、反応圧力：１〜２５ＭＰａ、ＬＨＳＶ（液空間速度）：０．１〜３０ｈ−１、Ｈ２／Ｏｉｌ（水素／油比）：２０〜５０００Ｌ／Ｌである。 Hydrorefining involves contacting the treated oil with a hydrorefining catalyst in the presence of hydrogen. As the hydrorefining catalyst, a catalyst in which at least one of molybdenum, nickel, cobalt, and phosphorus is supported on an inorganic porous carrier such as alumina, and particularly at least one of molybdenum and nickel or cobalt is preferably used. Preferred reaction conditions are: reaction temperature: 250 to 450 ° C., reaction pressure: 1 to 25 MPa, LHSV (liquid space velocity): 0.1 to 30 h −1 , H 2 / Oil (hydrogen / oil ratio): 20 to 5000 L / L It is.

水素化精製の後に残さ油とナフサ留分、灯油留分、軽油留分、重質軽油留分などの留分に分けられ、そのまま、または、他の石油精製工程を経て、石化用ナフサ、ガソリン、灯油、軽油、重油などの製品または製品を構成する基材となる。特に、石化用ナフサ、ガソリン基材としては、硫黄分１０ｐｐｍ以下、特には２ｐｐｍ以下、窒素分１０ｐｐｍ以下、特には２ｐｐｍ以下、塩素分１０ｐｐｍ以下特には１ｐｐｍ以下、全酸価０．０１ｍｇＫＯＨ／ｇ以下、ジエン価０．２ｇ／１００ｇ以下、特に０．１ｇ／１００ｇ以下とすることができる。   After hydrorefining, it is divided into fractions such as residual oil and naphtha fraction, kerosene fraction, light oil fraction, heavy gas oil fraction, etc. A product such as kerosene, light oil, heavy oil or a base material constituting the product. Especially for petrochemical naphtha and gasoline base, sulfur content is 10ppm or less, especially 2ppm or less, nitrogen content is 10ppm or less, especially 2ppm or less, chlorine content is 10ppm or less, especially 1ppm or less, and total acid value is 0.01mgKOH / g or less. The diene value can be 0.2 g / 100 g or less, particularly 0.1 g / 100 g or less.

実施例で用いたプラスチック分解油及び原油由来成分の性状を表１にまとめる。プラスチック分解油は、容器包装プラスチック油化事業者協議会より入手した。原油由来成分１は中東系原油を常圧蒸留された残さ油及び原油由来成分２はその残さ油を減圧蒸留して得られた減圧残さ油成分である。   Table 1 summarizes the properties of the plastic cracked oil and crude oil-derived components used in the examples. The plastic decomposition oil was obtained from the Containers and Packaging Plastic Oil Refinery Association. Crude oil-derived component 1 is a residue oil obtained by atmospheric distillation of Middle Eastern crude oil, and crude oil-derived component 2 is a vacuum residue oil component obtained by distilling the residue oil under reduced pressure.


表１の原油由来成分とプラスチック分解油を表２に示す割合で配合して混合原料油を用意した。この原料油を次の条件で水素化精製した。   The crude oil-derived component of Table 1 and the plastic decomposition oil were blended in the proportions shown in Table 2 to prepare a mixed raw material oil. This feedstock was hydrorefined under the following conditions.


混合原料油は、上下方向長さ１１６０ｍｍ、内径１９ｍｍの固定床流通式反応器中に、上から順に、３φのアルミナボール約１００ｍｌと、６０ｍｌ（４９．２ｇ）の水素化精製触媒（ＡＲＴ社製 ＨＯＰ８０２）と、３φアルミナボール約２５ｍｌを充填した中に、水素と共に上端から導入した。反応条件は、温度：４００℃、圧力１２．０ＭＰａ、ＬＨＳＶ：０．４ｈ−１、Ｈ２／Ｏｉｌ：４８００Ｌ／Ｌの条件下にて水素化精製を行った。用いたＡＲＴ社製ＨＯＰ８０２は、アルミナを担体として金属としてモリブデンを８ｗｔ％、ニッケルを２．２ｗｔ％含有しているものである。 In a fixed bed flow reactor having a vertical length of 1160 mm and an inner diameter of 19 mm, the mixed raw material oil was placed in order from the top, about 100 ml of 3φ alumina balls and 60 ml (49.2 g) of hydrorefining catalyst (manufactured by ART). HOP802) and about 25 ml of 3φ alumina balls were charged and introduced from the upper end together with hydrogen. The reaction conditions were hydrorefining under the conditions of temperature: 400 ° C., pressure: 12.0 MPa, LHSV: 0.4 h −1 , H 2 / Oil: 4800 L / L. The used HOP802 manufactured by ART contains 8 wt% molybdenum and 2.2 wt% nickel using alumina as a carrier as a metal.

反応器からの流出物を蒸留し、ナフサ留分、灯油留分、軽油留分、重質軽油留分の留分と残さ油とに分離する。   The effluent from the reactor is distilled and separated into a naphtha fraction, a kerosene fraction, a light oil fraction, a heavy gas oil fraction and a residual oil.

本発明は、特定の性状からなるプラスチック分解油を、特定の性状からなる原油由来成分と混合して、石油精製工程で処理するものであり、石油精製工程において、汚れ、コーキングなどの問題を生じることなく処理することが可能となり、特に、水素化精製処理により塩素分、窒素分など不純物を低減できる。したがって、不純物含有量の少ないプラスチック分解油を得ることができ、ガソリン基材原料や石油化学原料、灯軽油および重油基材として利用することができる。
In the present invention, a plastic cracked oil having a specific property is mixed with a crude oil-derived component having a specific property and processed in an oil refining process, which causes problems such as dirt and coking in the oil refining process. In particular, the hydrorefining treatment can reduce impurities such as chlorine and nitrogen. Accordingly, it is possible to obtain a plastic cracked oil having a small impurity content, and it can be used as a gasoline base material, petrochemical raw material, kerosene oil, and heavy oil base material.

Claims (7)

プラスチックの分解によって生成するプラスチック分解油を原油由来成分と混合し、石油精製工程において処理するプラスチック分解油処理方法であって、
前記原油由来成分の９０％留出温度が、前記プラスチック分解油の９０％留出温度以上であるプラスチック分解油処理方法。 A plastic cracked oil treatment method in which a plastic cracked oil produced by cracking plastic is mixed with a crude oil-derived component and processed in a petroleum refining process,
A method for treating plastic cracked oil, wherein a 90% distillation temperature of the crude oil-derived component is equal to or higher than a 90% distillation temperature of the plastic cracked oil. 前記原油由来成分の９０％留出温度が、２００℃以上である請求項１に記載のプラスチック分解油処理方法。 The method for treating plastic cracked oil according to claim 1, wherein a 90% distillation temperature of the crude oil-derived component is 200 ° C or higher. 前記原油由来成分が残さ油である請求項１又は２に記載のプラスチック分解油処理方法。 The method for treating plastic cracked oil according to claim 1 or 2, wherein the crude oil-derived component is residual oil. 前記プラスチック分解油の１０％留出温度が２００℃未満である請求項１〜３のいずれかに記載のプラスチック分解油処理方法。 The method for treating plastic cracked oil according to any one of claims 1 to 3, wherein a 10% distillation temperature of the plastic cracked oil is less than 200 ° C. 前記プラスチック分解油は、初留点が１００℃未満である請求項１〜４のいずれかに記載のプラスチック分解油処理方法。 The plastic cracked oil treatment method according to any one of claims 1 to 4, wherein the plastic cracked oil has an initial boiling point of less than 100 ° C. 前記プラスチック分解油の９０％留出温度が３００℃を超え、６００℃以下である請求項１〜５のいずれかに記載のプラスチック分解油処理方法。 The method for treating plastic cracked oil according to any one of claims 1 to 5, wherein a 90% distillation temperature of the plastic cracked oil is higher than 300 ° C and not higher than 600 ° C. 前記石油精製工程は、水素化精製、水素化分解及び接触分解の少なくとも一つの工程を含むことを特徴とする請求項１〜６のいずれかに記載のプラスチック分解油処理方法。
The method for treating plastic cracked oil according to any one of claims 1 to 6, wherein the petroleum refining step includes at least one step of hydrorefining, hydrocracking, and catalytic cracking.
JP2005315547A 2005-10-31 2005-10-31 Processing method of plastic decomposition oil Expired - Fee Related JP4787598B2 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP2005315547A JP4787598B2 (en) 2005-10-31 2005-10-31 Processing method of plastic decomposition oil

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP2005315547A JP4787598B2 (en) 2005-10-31 2005-10-31 Processing method of plastic decomposition oil

Publications (2)

Publication Number Publication Date
JP2007119648A true JP2007119648A (en) 2007-05-17
JP4787598B2 JP4787598B2 (en) 2011-10-05

Family

ID=38143824

Family Applications (1)

Application Number Title Priority Date Filing Date
JP2005315547A Expired - Fee Related JP4787598B2 (en) 2005-10-31 2005-10-31 Processing method of plastic decomposition oil

Country Status (1)

Country Link
JP (1) JP4787598B2 (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017512246A (en) * 2014-02-25 2017-05-18 サウジ ベーシック インダストリーズ コーポレイションＳａｕｄｉ Ｂａｓｉｃ Ｉｎｄｕｓｔｒｉｅｓ Ｃｏｒｐｏｒａｉｔｏｎ Method of converting mixed waste plastics (MWP) into valuable petrochemical products
ES2769963A1 (en) * 2018-12-28 2020-06-29 Neste Oyj Coprocessing method (Machine-translation by Google Translate, not legally binding)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023222550A1 (en) * 2022-05-20 2023-11-23 Unilever Ip Holdings B.V. Methods for producing ingredients from waste plastic pyrolysis oil

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10310778A (en) * 1997-05-12 1998-11-24 Mitsubishi Oil Co Ltd Purification of oil made from waste plastic and purified fraction
JP2005272759A (en) * 2004-03-26 2005-10-06 Japan Energy Corp Method for treating plastic cracked oil

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10310778A (en) * 1997-05-12 1998-11-24 Mitsubishi Oil Co Ltd Purification of oil made from waste plastic and purified fraction
JP2005272759A (en) * 2004-03-26 2005-10-06 Japan Energy Corp Method for treating plastic cracked oil

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017512246A (en) * 2014-02-25 2017-05-18 サウジ ベーシック インダストリーズ コーポレイションＳａｕｄｉ Ｂａｓｉｃ Ｉｎｄｕｓｔｒｉｅｓ Ｃｏｒｐｏｒａｉｔｏｎ Method of converting mixed waste plastics (MWP) into valuable petrochemical products
US10233395B2 (en) 2014-02-25 2019-03-19 Saudi Basic Industries Corporation Process for converting mixed waste plastic (MWP) into valuable petrochemicals
ES2769963A1 (en) * 2018-12-28 2020-06-29 Neste Oyj Coprocessing method (Machine-translation by Google Translate, not legally binding)
DE102019133911B4 (en) 2018-12-28 2022-05-19 Neste Oyj Methods of co-processing

Also Published As

Publication number Publication date
JP4787598B2 (en) 2011-10-05

Similar Documents

Publication Publication Date Title
US20230287282A1 (en) Purification of waste plastic based oil with a high temperature hydroprocessing
KR102457860B1 (en) Systems and methods for converting feedstock hydrocarbons into petrochemicals
US8173009B2 (en) Process for improving a hydrotreated stream
JP2024501716A (en) Co-processing route for hydroprocessing polymer waste-based materials
JP2009179795A (en) Crude oil desulfurization
WO2014003943A1 (en) Decontamination of deoxygenated biomass-derived pyrolysis oil using ionic liquids
WO2017019744A1 (en) Integrated ebullated-bed hydroprocessing, fixed bed hydroprocessing and coking process for whole crude oil conversion into hydrotreated distillates and petroleum green coke
JP4787598B2 (en) Processing method of plastic decomposition oil
NL2024523B1 (en) Method for co-processing
JP5246996B2 (en) Processing method of plastic decomposition oil
JP2011042734A (en) Method for producing highly aromatic hydrocarbon oil
JP4382552B2 (en) Processing method of plastic decomposition oil
JP7466067B2 (en) Method for treating liquefied waste polymers - Patents.com
US20110180456A1 (en) Integrated Process and System for Steam Cracking and Catalytic Hydrovisbreaking with Catalyst Recycle
KR101804663B1 (en) Method of Preparing Hydroprocessing Catalysts from in Waste Oil and Method of Converting Heavy oil using the same
JP4236548B2 (en) Production method of naphtha fraction
CN114437764B (en) Desilication method and system for siliceous hydrocarbon raw material
WO2015147084A1 (en) Method for producing xylene
WO2011090532A1 (en) Integrated process and system for steam cracking and catalytic hydrovisbreaking with catalyst recycle
EP4055121A1 (en) Process for the preparation of olefins, comprising de-asphalting, hydrocracking and steam cracking
KR20230063995A (en) Device and method for refining waste plastic pyrolysis oil
JP5207923B2 (en) Process for producing refined hydrocarbon oil
CN117004433A (en) Method for dechlorinating waste plastic oil and/or waste tire oil
JP2010111770A (en) Method for producing purified hydrocarbon oil, and purified hydrocarbon oil
JP2010111771A (en) Method for producing purified hydrocarbon oil, and purified hydrocarbon oil

Legal Events

Date Code Title Description
RD04 Notification of resignation of power of attorney

Free format text: JAPANESE INTERMEDIATE CODE: A7424

Effective date: 20070725

A621 Written request for application examination

Free format text: JAPANESE INTERMEDIATE CODE: A621

Effective date: 20080911

A711 Notification of change in applicant

Free format text: JAPANESE INTERMEDIATE CODE: A712

Effective date: 20101129

A131 Notification of reasons for refusal

Free format text: JAPANESE INTERMEDIATE CODE: A131

Effective date: 20110427

A977 Report on retrieval

Free format text: JAPANESE INTERMEDIATE CODE: A971007

Effective date: 20110427

A521 Request for written amendment filed

Free format text: JAPANESE INTERMEDIATE CODE: A523

Effective date: 20110620

TRDD Decision of grant or rejection written
A01 Written decision to grant a patent or to grant a registration (utility model)

Free format text: JAPANESE INTERMEDIATE CODE: A01

Effective date: 20110706

A01 Written decision to grant a patent or to grant a registration (utility model)

Free format text: JAPANESE INTERMEDIATE CODE: A01

A61 First payment of annual fees (during grant procedure)

Free format text: JAPANESE INTERMEDIATE CODE: A61

Effective date: 20110715

R150 Certificate of patent or registration of utility model

Ref document number: 4787598

Country of ref document: JP

Free format text: JAPANESE INTERMEDIATE CODE: R150

Free format text: JAPANESE INTERMEDIATE CODE: R150

FPAY Renewal fee payment (event date is renewal date of database)

Free format text: PAYMENT UNTIL: 20140722

Year of fee payment: 3

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

S531 Written request for registration of change of domicile

Free format text: JAPANESE INTERMEDIATE CODE: R313531

S533 Written request for registration of change of name

Free format text: JAPANESE INTERMEDIATE CODE: R313533

R350 Written notification of registration of transfer

Free format text: JAPANESE INTERMEDIATE CODE: R350

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

S533 Written request for registration of change of name

Free format text: JAPANESE INTERMEDIATE CODE: R313533

R350 Written notification of registration of transfer

Free format text: JAPANESE INTERMEDIATE CODE: R350

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

S533 Written request for registration of change of name

Free format text: JAPANESE INTERMEDIATE CODE: R313533

R350 Written notification of registration of transfer

Free format text: JAPANESE INTERMEDIATE CODE: R350

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

LAPS Cancellation because of no payment of annual fees