JPH0948983A - Production of refined oil from decomposed oil of waste plastics - Google Patents
Production of refined oil from decomposed oil of waste plasticsInfo
- Publication number
- JPH0948983A JPH0948983A JP22106695A JP22106695A JPH0948983A JP H0948983 A JPH0948983 A JP H0948983A JP 22106695 A JP22106695 A JP 22106695A JP 22106695 A JP22106695 A JP 22106695A JP H0948983 A JPH0948983 A JP H0948983A
- Authority
- JP
- Japan
- Prior art keywords
- oil
- decomposed
- catalyst
- refined
- waste plastics
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/62—Plastics recycling; Rubber recycling
Landscapes
- Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は廃プラスチック（こ
こで、「プラスチック」はエラストマー類、ワックス
類、グリース類等の狭義には樹脂に属しないとされ得る
重合体類をも包含する）、特に廃合成プラスチックの分
解によって得られる油状物から精製油を製造する方法に
関する。詳しくは、本発明は前記の油状物を触媒の存在
下に水素化処理して分解油中の窒素含有化合物及び／又
は塩素含有化合物を除去することからなる精製油の製造
方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to waste plastics (here, "plastics" include polymers such as elastomers, waxes, greases, etc., which can be regarded as not belonging to a resin in a narrow sense), The present invention relates to a method for producing a refined oil from an oily substance obtained by decomposing waste synthetic plastic. More specifically, the present invention relates to a method for producing a refined oil, which comprises hydrotreating the oily substance in the presence of a catalyst to remove nitrogen-containing compounds and / or chlorine-containing compounds in cracked oil.
【０００２】[0002]
【従来の技術】ポリオレフィン類は分解によって容易に
油状化され得る。その結果として廃プラスチックを分解
して得られる油状物の中には往々にして窒素含有化合物
及び／又は塩素含有化合物が含有される。その原因は分
解原料である廃プラスチック中に往々にして含有される
窒素含有重合体例えば、各種ナイロン類、ポリウレタン
類、ＡＢＳ樹脂及びＮＢＲ及び／又は塩素含有重合体例
えば、ポリ塩化ビニル（ＰＶＣ）、ポリ塩化ビニリデン
（ＰＶＤＣ）及び／又は塩素化ポリエチレンに帰すこと
ができる。Polyolefins can be easily oiled by decomposition. As a result, nitrogen-containing compounds and / or chlorine-containing compounds are often contained in the oily product obtained by decomposing waste plastic. The cause is nitrogen-containing polymers, such as various nylons, polyurethanes, ABS resins and NBR and / or chlorine-containing polymers, such as polyvinyl chloride (PVC), which are often contained in waste plastics which are decomposition raw materials. It can be attributed to polyvinylidene chloride (PVDC) and / or chlorinated polyethylene.
【０００３】[0003]
【発明が解決しようとする課題】得られる油状物の有効
利用を妨げる原因となっているものは分解原料である廃
プラスチック中に通常は或割合で含有されるナイロン類
から発生する窒素化合物、ポリ塩化ビニル樹脂、ポリ塩
化ビニリデン樹脂又は塩素化ポリエチレン等から発生す
る塩素化合物であることが既に判っている。What has been the cause of hindering the effective use of the obtained oily substance is nitrogen compounds, polynitrogens, generated from nylons, which are usually contained in a certain proportion in the waste plastic which is a decomposition raw material. It has already been known that it is a chlorine compound generated from vinyl chloride resin, polyvinylidene chloride resin, chlorinated polyethylene or the like.
【０００４】しかし、上記の油状物から窒素化合物及び
／又は塩素化合物を効果的で経済的に除去する方法が判
らなかったことに起因して、分解油は辛うじて燃料油と
して用いられて来た程度である。However, cracked oil has barely been used as a fuel oil due to the fact that a method for effectively and economically removing nitrogen compounds and / or chlorine compounds from the above oily substance has not been found. Is.
【０００５】[0005]
【課題を解決するための手段】本発明者は廃プラスチッ
クの分解によって得られる分解油から窒素含有化合物及
び／又は塩素含有化合物を分解除去して各種の用途に用
いられ得る精製油を得る為の精製方法を広範に検討した
結果、下記の精製方法を完成した：廃プラスチックの分
解生成物である分解油を触媒の存在下に水素で還元処理
することによって油中に含有されている窒素含有化合物
及び塩素含有化合物の少なくとも何れかを分解除去する
精製油の製造方法。DISCLOSURE OF THE INVENTION The inventor of the present invention provides a refined oil that can be used for various purposes by decomposing and removing nitrogen-containing compounds and / or chlorine-containing compounds from decomposed oil obtained by decomposing waste plastics. As a result of extensive investigation of the refining method, the following refining method has been completed: Nitrogen-containing compound contained in oil by reducing hydrogenated cracked oil, which is a decomposition product of waste plastic, in the presence of a catalyst. And a method for producing a refined oil by decomposing and removing at least one of a chlorine-containing compound.
【０００６】[0006]
＜分解原料となる廃プラスチック＞本発明における分解
油の原料となる重合体廃棄物特に、廃プラスチックは各
種のものを包含しており例えば、熱可塑性樹脂及び熱硬
化性樹脂の何れをも包含し得る。<Waste plastic used as a decomposition raw material> Polymer waste used as a raw material for decomposed oil in the present invention. In particular, waste plastics include various kinds, for example, both thermoplastic resins and thermosetting resins. obtain.
【０００７】熱可塑性樹脂としてはポリオレフィン（Ｐ
Ｏ）例えば、ポリエチレン（ＰＥ）、ポリプロピレン
（ＰＰ）、スチレン系樹脂例えば、ポリスチレン（Ｐ
Ｓ）、耐衝撃性ポリスチレン（ＨＩＰＳ）、窒素含有樹
脂例えば、ポリアミド樹脂（別名「ナイロン」）、ＡＢ
Ｓ樹脂、オレフィンモノマーと小割合の別種モノマーと
の共重合樹脂例えば、エチレン−酢酸ビニル共重合樹脂
（ＥＶＡ）、塩素含有樹脂例えば、ポリ塩化ビニル（Ｐ
ＶＣ）、ポリ塩化ビニリデン（ＰＶＤＣ）及び別種樹脂
であるポリカーボネート（ＰＣ）等並びに熱硬化性樹脂
であるフェノール樹脂、メラミン樹脂、尿素樹脂、アル
キッド樹脂及びポリウレタン（ＰＵ）等の何れかが単独
でも又は２種以上の混合物であっても差支え無い。As the thermoplastic resin, polyolefin (P
O) For example, polyethylene (PE), polypropylene (PP), styrene resin such as polystyrene (P
S), high impact polystyrene (HIPS), nitrogen-containing resins such as polyamide resin (also known as “nylon”), AB
S resin, a copolymer resin of an olefin monomer and a small proportion of another monomer such as ethylene-vinyl acetate copolymer resin (EVA), a chlorine-containing resin such as polyvinyl chloride (P
VC), polyvinylidene chloride (PVDC) and another type of polycarbonate (PC), and thermosetting resin such as phenol resin, melamine resin, urea resin, alkyd resin and polyurethane (PU) alone or It does not matter even if it is a mixture of two or more kinds.
【０００８】なお、本発明方法の分解原料である合成重
合体とは、合成樹脂に限らず軟質の重合体、共重合体及
びそれらの２種以上の組成物等を広範に包含する重合体
であって、その典型的例を下記に挙げる： ◆エチレン系ワックス状重合体もしくはグリース状重合
体、 ◆プロピレン系ワックス状重合体もしくはグリース状重
合体例えばアタクチックポリプロピレン又は ◆合成ゴム例えばエチレン−プロピレン共重合ゴム（Ｅ
ＰＭ）、エチレン−プロピレン−非共役ジエン共重合ゴ
ム（ＥＰＤＭ）、スチレン−ブタジエン共重合ゴム（Ｓ
ＢＲ）、ブタジエン−アクリロニトリル共重合体ゴム
（ＮＢＲ）、クロロプレンゴム（ＣＲ）、ポリイソプレ
ンゴム（ＩＲ）、ブチルゴム（ＩＩＲ）、ポリブタジエ
ンゴム（ＢＲ）及びそれらの架橋物（加硫物）、熱可塑
性エラストマー例えばエチレン−プロピレン−非共役ジ
エン共重合ゴム／ポリエチレン組成物の部分架橋物、ス
チレン−ブタジエン共重合体水素化物及び通称「石油樹
脂」等の合成「炭化水素樹脂」をも包含する。The synthetic polymer used as the decomposition raw material in the method of the present invention is not limited to synthetic resins, but is a polymer including a wide range of soft polymers, copolymers, and compositions of two or more thereof. Therefore, typical examples thereof are as follows: ◆ ethylene wax polymer or grease polymer, ◆ propylene wax polymer or grease polymer such as atactic polypropylene, ◆ synthetic rubber such as ethylene-propylene copolymer Polymerized rubber (E
PM), ethylene-propylene-non-conjugated diene copolymer rubber (EPDM), styrene-butadiene copolymer rubber (S
BR), butadiene-acrylonitrile copolymer rubber (NBR), chloroprene rubber (CR), polyisoprene rubber (IR), butyl rubber (IIR), polybutadiene rubber (BR) and their crosslinked products (vulcanized products), thermoplasticity Elastomers such as partially crosslinked products of ethylene-propylene-non-conjugated diene copolymer rubber / polyethylene composition, styrene-butadiene copolymer hydrides and synthetic "hydrocarbon resins" such as commonly known as "petroleum resins" are also included.
【０００９】特に、分解原料中に或程度の量で低融点重
合体例えば、アタクチックポリプロピレンが共存するこ
とは本発明方法の実施にとって好ましい。その理由は分
解装置において本発明方法を実施する際に該重合体が先
ず溶融して、分解に先立って生ずるべき変化である分解
原料重合体の溶融又は細分を助ける働きをすることにあ
る。即ち、溶融した低融点重合体が本命の分解原料重合
体の表面に密着して熱エネルギーを効果的に伝達する結
果、本命重合体の溶融に必要なエネルギーを節減する役
割を果たすことが期待され得る。In particular, it is preferable for carrying out the method of the present invention that a low melting point polymer such as atactic polypropylene is present in the decomposition raw material in a certain amount. The reason is that when the method of the present invention is carried out in a cracking apparatus, the polymer is first melted and serves to aid the melting or subdividing of the cracked starting polymer which is the change which should occur prior to cracking. That is, it is expected that the melted low melting point polymer will adhere to the surface of the favorite raw material polymer for decomposition to effectively transfer heat energy, and as a result, it will play a role of saving the energy required for melting the favorite polymer. obtain.
【００１０】本発明方法の原料として特に好ましい合成
重合体はポリエチレン、ポリプロピレン等のポリオレフ
ィン及び２種以上のオレフィン重合体の組成物並びにそ
れらの成分モノマーの共重合体を主成分とするものであ
る。A particularly preferred synthetic polymer as a raw material for the method of the present invention is a composition containing polyolefin such as polyethylene and polypropylene and a composition of two or more kinds of olefin polymers, and a copolymer of those component monomers as a main component.
【００１１】他方、分解原料中には多くの場合に窒素含
有重合体及び／又は塩素含有重合体が混在する。混在重
合体としては例えば、下記の様な重合体（「樹脂」及び
「ゴム」、別名「結晶性重合体」及び「非晶性もしくは
低結晶性重合体」を包含する）を挙げることができる： ◆窒素含有重合体としてポリアミド樹脂（別名「ナイロ
ン」）、ＡＢＳ樹脂、ブタジエン−アクリロニトリル共
重合体ゴム（ＮＢＲ）； ◆塩素含有重合体例えば、ポリ塩化ビニル（ＰＶＣ）、
ポリ塩化ビニリデン（ＰＶＤＣ）、クロロプレンゴム
（ＣＲ）、上記の窒素含有重合体及び／又は塩素含有重
合体が通常０.１〜２０重量％、好ましくは１〜１０重
量％（全重合体量基準）混在する原料プラスチックに対
して本発明方法が著効を発揮する。On the other hand, a nitrogen-containing polymer and / or a chlorine-containing polymer are mixed in the decomposition raw material in many cases. Examples of the mixed polymer include the following polymers (including "resin" and "rubber", also known as "crystalline polymer" and "amorphous or low crystalline polymer"). Polyamide resin (also known as “nylon”), ABS resin, butadiene-acrylonitrile copolymer rubber (NBR) as nitrogen-containing polymer; Chlorine-containing polymer such as polyvinyl chloride (PVC),
Polyvinylidene chloride (PVDC), chloroprene rubber (CR), the above-mentioned nitrogen-containing polymer and / or chlorine-containing polymer is usually 0.1 to 20% by weight, preferably 1 to 10% by weight (based on the total amount of the polymer). The method of the present invention is very effective for mixed raw material plastics.
【００１２】＜水素化触媒＞本発明の精製方法において
用いられる触媒は水素化触媒であって、石油の接触水素
化精製において用いられる遷移金属の酸化物触媒と同一
物で十分である。触媒としては例えば、酸化モリブデ
ン、酸化ニッケル及び酸化コバルトから選ばれる１種以
上である。更に、これらの遷移金属酸化物が固体酸であ
るアルミナ、シリカ、シリカアルミナ、チタニア及びゼ
オライトの１種以上並びに固体塩基であるマグネシアか
ら選ばれる１種以上からなる適切な微粒子担体表面に担
持されたものは触媒効率の点で好ましい。即ち、触媒性
能を発揮する遷移金属酸化物が担体表面に選択的に分布
し得ることから、所定量の触媒を可能な限り効率的に活
用することができる。<Hydrogenation Catalyst> The catalyst used in the refining method of the present invention is a hydrogenation catalyst, and the same one as the transition metal oxide catalyst used in the catalytic hydrorefining of petroleum is sufficient. The catalyst is, for example, one or more selected from molybdenum oxide, nickel oxide and cobalt oxide. Further, these transition metal oxides are supported on a suitable fine particle carrier surface comprising one or more kinds of solid acids such as alumina, silica, silica-alumina, titania and zeolite and one or more kinds selected from magnesia which is a solid base. Those are preferable in terms of catalyst efficiency. That is, since the transition metal oxide exhibiting catalytic performance can be selectively distributed on the surface of the support, a predetermined amount of catalyst can be utilized as efficiently as possible.
【００１３】本発明の精製方法において所期の効果を発
現させるに好ましい態様としては、上記の各種遷移金属
酸化物触媒を固体酸及び／又は固体塩基からなり、次記
の性状を備えた粉末に担持させて用いる。本発明方法に
おける担体としては平均粒径域５０〜５００００μm、
好ましくは５００〜５０００μm、比表面積（ＢＥＴ法
による）０.１〜１０００m2/g、好ましくは１０〜３０
０m2/gのものが用いられる。In a preferred embodiment for producing the desired effect in the purification method of the present invention, the above-mentioned various transition metal oxide catalysts are formed into a powder having a solid acid and / or a solid base and having the following properties. Used by supporting. The carrier in the method of the present invention has an average particle size range of 50 to 50,000 μm,
Preferably 500-5000 μm, specific surface area (by BET method) 0.1-1000 m 2 / g, preferably 10-30
The one of 0 m 2 / g is used.
【００１４】＜操作条件＞本発明の精製方法は上記の触
媒の存在下に分解油中にその１kg当たり触媒（遷移金属
酸化物基準）５〜５００g、好ましくは２０〜２００gの
存在下に水素をその分圧０.５〜１５MPa、好ましくは１
〜１０MPa (NTP)で存在させた状態で反応系を温度２０
０〜６００℃、好ましくは２５０〜４５０℃に通常０.
５〜１０h、好ましくは１〜３h加熱して窒素含有化合物
及び／又は塩素含有化合物を分解除去する方法である。<Operating conditions> In the refining method of the present invention, hydrogen is added to cracked oil in the presence of the above catalyst in an amount of 5 to 500 g, preferably 20 to 200 g of catalyst (based on transition metal oxide) per 1 kg thereof. The partial pressure is 0.5 to 15 MPa, preferably 1
The reaction system was heated at a temperature of 20 MPa in the presence of 10 MPa (NTP).
Usually 0 to 0 to 600 ° C, preferably 250 to 450 ° C.
It is a method of decomposing and removing the nitrogen-containing compound and / or the chlorine-containing compound by heating for 5 to 10 hours, preferably 1 to 3 hours.
【００１５】上記の本発明の精製は各種の反応方式（装
置）例えば、（槽型）バッチ反応方式、固定床方式、管
型反応方式、流動床方式又は移動床方式等を用いて行な
うことができる。The above-mentioned purification of the present invention can be carried out using various reaction systems (apparatuses) such as (tank type) batch reaction system, fixed bed system, tubular reaction system, fluidized bed system or moving bed system. it can.
【００１６】本発明の精製方法によって精製された油状
物は次に、ナフサクラッキングと同一の処理によって石
油化学原料として有用なエチレン、プロピレン、1-ブテ
ン、ブタジエン、イソプレン、ベンゼン、トルエン、キ
シレン、スチレンその他の不飽和炭化水素へ変換され得
る。変換によって得られる不飽和炭化水素の中でも、エ
チレン及びプロピレンが広汎な製品の原料となり得る点
で好ましい。The oil refined by the refining method of the present invention is then treated with ethylene, propylene, 1-butene, butadiene, isoprene, benzene, toluene, xylene and styrene which are useful as petrochemical raw materials by the same treatment as naphtha cracking. It can be converted to other unsaturated hydrocarbons. Among the unsaturated hydrocarbons obtained by the conversion, ethylene and propylene are preferable because they can be raw materials for a wide range of products.
【００１７】本発明の精製方法によって達成された効果
を確認する為の定量分析は下記の分析装置を用いて行な
った： ◆窒素含有化合物の定量：微量全窒素分析装置（三菱化
学社製） ◆塩素含有化合物の定量：全塩素分析装置ＴＳＸ−１０
型（三菱化学社製）。Quantitative analysis for confirming the effect achieved by the purification method of the present invention was carried out using the following analyzers: ◆ Quantification of nitrogen-containing compounds: trace total nitrogen analyzer (manufactured by Mitsubishi Chemical Co.) ◆ Determination of chlorine-containing compound: Total chlorine analyzer TSX-10
Mold (manufactured by Mitsubishi Chemical).
【００１８】[0018]
【発明の効果】本発明の精製方法によれば、(１)廃プラ
スチックの分解によって生成する分解油から効果的にし
かも経済的に窒素含有化合物及び／又は塩素含有化合物
を分解除去して精製油を得ることができる、(２)更にそ
の精製油をスチームクラッキング処理することによって
石油化学原料に使用可能な純度のエチレン、プロピレン
等の1-オレフィン、ブタジエン、イソプレン等の共役ジ
オレフィンを再生することもできる。According to the refining method of the present invention, (1) a refined oil obtained by decomposing and removing a nitrogen-containing compound and / or a chlorine-containing compound from the decomposed oil produced by decomposing waste plastics effectively and economically. (2) The refined oil is further steam-cracked to regenerate 1-olefins such as ethylene and propylene and conjugated diolefins such as butadiene and isoprene with a purity that can be used as petrochemical raw materials. You can also
【００１９】[0019]
【実施例１】精製装置として耐食鋼製のオートクレーブ
（内容積１００ml）内に遷移金属触媒［酸化モリブデン
２０重量％、酸化ニッケル３重量％及び酸化コバルト５
重量％からなる複合体がγ-アルミナ担体（球状；平均
直径１mm）７２重量％に担持されたもの］３g、廃ポリ
プロピレン分解油（窒素含有量１５０ppm及び塩素含有
量２５０ppm）３０g並びに水素２MPaを装入して水素化
反応を温度３８０℃で３h行なった。オートクレーブか
ら取り出された油を分析した結果、窒素含有量６ppm及
び塩素含有量２ppmであることが判った。Example 1 As a refining device, a transition metal catalyst [20 wt% molybdenum oxide, 3 wt% nickel oxide and 5 cobalt oxide] was placed in a corrosion-resistant steel autoclave (internal volume 100 ml).
72% by weight of γ-alumina carrier (spherical; average diameter 1 mm) containing 3% by weight of composite] 3 g of waste polypropylene decomposed oil (nitrogen content 150 ppm and chlorine content 250 ppm) and hydrogen 2 MPa. Then, the hydrogenation reaction was carried out at a temperature of 380 ° C. for 3 hours. Analysis of the oil taken from the autoclave revealed a nitrogen content of 6 ppm and a chlorine content of 2 ppm.
【００２０】[0020]
【実施例２】精製装置として耐食鋼製のオートクレーブ
（内容積１００ml）内に遷移金属触媒［酸化モリブデン
２０重量％及び酸化コバルト５重量％からなる複合体が
珪藻土担体（球状；平均直径１mm）７５重量％に担持さ
れたもの］５g、廃ポリプロピレン分解油（窒素含有量
１５０ppm及び塩素含有量２５０ppm）３０g並びに水素
４MPaを装入して水素化反応を温度３８０℃で２h行なっ
た。オートクレーブから取り出された油を分析した結
果、窒素含有量４ppm及び塩素含有量１ppmであることが
判った。[Example 2] As a refining apparatus, a transition metal catalyst [a complex consisting of 20% by weight of molybdenum oxide and 5% by weight of cobalt oxide was used as a diatomaceous earth carrier (spherical; average diameter 1 mm) in an autoclave made of corrosion-resistant steel (internal volume: 100 ml). 5 g, which was carried in wt%], 30 g of waste polypropylene decomposed oil (150 ppm nitrogen content and 250 ppm chlorine content) and 4 MPa hydrogen were charged and the hydrogenation reaction was carried out at a temperature of 380 ° C. for 2 hours. Analysis of the oil taken from the autoclave revealed a nitrogen content of 4 ppm and a chlorine content of 1 ppm.
【００２１】[0021]
【実施例３】精製装置として耐食鋼製のオートクレーブ
（内容積１００ml）内に遷移金属触媒［酸化モリブデン
２０重量％、酸化ニッケル３重量％及び酸化コバルト５
重量％からなる複合体２gがシリカ-アルミナ担体（球
状；平均直径２mm）７２重量％に担持されたもの］２
g、廃プラスチック分解油（窒素含有量６８０ppm及び塩
素含有量３６０ppm）３０g並びに水素２MPaを装入して
水素化反応を温度５２０℃で１h行なった。オートクレ
ーブから取り出された油を分析した結果、窒素含有量８
ppm及び塩素含有量２ppmであることが判った。[Example 3] As a refining device, a transition metal catalyst [20% by weight of molybdenum oxide, 3% by weight of nickel oxide and 5% of cobalt oxide] was placed in an autoclave made of corrosion resistant steel (internal volume: 100 ml).
2 g of a composite of 2 wt% was supported on 72 wt% of silica-alumina carrier (spherical; average diameter 2 mm)] 2
g, 30 g of waste plastic decomposition oil (nitrogen content 680 ppm and chlorine content 360 ppm) and 2 MPa of hydrogen were charged, and the hydrogenation reaction was carried out at a temperature of 520 ° C. for 1 hour. As a result of analyzing the oil taken out from the autoclave, the nitrogen content was 8
It was found to be ppm and a chlorine content of 2 ppm.
【００２２】[0022]
【実施例４】精製装置として耐食鋼製のオートクレーブ
（内容積１００ml）内に遷移金属触媒［酸化ニッケル２
０重量％及び酸化コバルト５重量％からなる複合体がシ
リカ-アルミナ担体（球状；平均直径２mm）７５重量％
に担持されたもの］５g、廃プラスチック分解油（窒素
含有量６８０ppm及び塩素含有量３６０ppm）３０g並び
に水素５MPaを装入して水素化反応を温度２５０℃で３h
行なった。オートクレーブから取り出された油を分析し
た結果、窒素含有量９ppm及び塩素含有量３ppmであるこ
とが判った。Example 4 As a refining device, a transition metal catalyst [nickel oxide 2 was placed in an autoclave (internal volume 100 ml) made of corrosion-resistant steel.
A composite consisting of 0 wt% and 5 wt% cobalt oxide is a silica-alumina carrier (spherical; average diameter 2 mm) 75 wt%
5g, waste plastic decomposed oil (nitrogen content 680ppm and chlorine content 360ppm) 30g and hydrogen 5MPa were charged to carry out hydrogenation reaction at a temperature of 250 ° C for 3 hours.
I did. Analysis of the oil taken from the autoclave revealed a nitrogen content of 9 ppm and a chlorine content of 3 ppm.
【００２３】[0023]
【実施例５】実施例１において製造された精製油を水蒸
気で１０容量倍に希釈し、得られた混合気体を温度８０
０℃、平均反応時間０.５minの条件下でスチームクラッ
キングした結果、エチレン収率２５重量％及びプロピレ
ン収率２１重量％が得られた。Example 5 The refined oil produced in Example 1 was diluted with steam to a volume of 10 times, and the resulting mixed gas was heated to a temperature of 80.
As a result of steam cracking under conditions of 0 ° C. and an average reaction time of 0.5 min, an ethylene yield of 25% by weight and a propylene yield of 21% by weight were obtained.
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｃ０７Ｃ 11/06 Ｃ０７Ｃ 11/06 Ｃ０８Ｊ 11/00 Ｃ０８Ｊ 11/00 11/10 11/10 11/14 11/14 Ｃ１０Ｇ 9/36 9279−4Ｈ Ｃ１０Ｇ 9/36 45/12 9547−4Ｈ 45/12 Ｚ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification code Internal reference number FI Technical display location C07C 11/06 C07C 11/06 C08J 11/00 C08J 11/00 11/10 11/10 11/14 11/14 C10G 9/36 9279-4H C10G 9/36 45/12 9547-4H 45/12 Z
Claims (5)
油を触媒の存在下に水素化処理することによって油中に
含有されている窒素含有化合物及び塩素含有化合物の少
なくとも何れかを分解除去する精製油の製造方法。1. Purification for decomposing and removing at least one of a nitrogen-containing compound and a chlorine-containing compound contained in oil by hydrotreating decomposed oil which is a decomposition product of waste plastic in the presence of a catalyst. Oil production method.
る請求項１に記載の精製油の製造方法。2. The method for producing a refined oil according to claim 1, wherein the treatment is performed at a temperature of 200 to 600 ° C.
又は２に記載の精製油の製造方法。3. The catalyst used is a transition metal-based catalyst.
Or the method for producing a refined oil according to item 2.
００gである請求項１〜３の何れかに記載の精製油の製
造方法。4. The amount of catalyst used is 5 to 5 per 1 kg of cracked oil.
It is 00 g, The manufacturing method of the refined oil in any one of Claims 1-3.
をエチレン製造プラントにおいてナフサ分解と同一条件
下にクラッキング処理するエチレン及びプロピレン等の
石油化学原料の製造方法。5. A method for producing a petrochemical raw material such as ethylene and propylene, wherein the refined oil obtained in any one of claims 1 to 4 is cracked in an ethylene production plant under the same conditions as naphtha cracking.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22106695A JPH0948983A (en) | 1995-08-07 | 1995-08-07 | Production of refined oil from decomposed oil of waste plastics |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP22106695A JPH0948983A (en) | 1995-08-07 | 1995-08-07 | Production of refined oil from decomposed oil of waste plastics |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0948983A true JPH0948983A (en) | 1997-02-18 |
Family
ID=16760964
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP22106695A Pending JPH0948983A (en) | 1995-08-07 | 1995-08-07 | Production of refined oil from decomposed oil of waste plastics |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0948983A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023096379A1 (en) * | 2021-11-26 | 2023-06-01 | Sk Innovation Co., Ltd. | Refining apparatus and refining method of waste plastic pyrolysis oil |
| US11999920B2 (en) | 2020-09-14 | 2024-06-04 | Ecolab Usa Inc. | Cold flow additives for plastic-derived synthetic feedstock |
| US12031097B2 (en) | 2022-10-12 | 2024-07-09 | Ecolab Usa Inc. | Antifouling agents for plastic-derived synthetic feedstocks |
-
1995
- 1995-08-07 JP JP22106695A patent/JPH0948983A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11999920B2 (en) | 2020-09-14 | 2024-06-04 | Ecolab Usa Inc. | Cold flow additives for plastic-derived synthetic feedstock |
| WO2023096379A1 (en) * | 2021-11-26 | 2023-06-01 | Sk Innovation Co., Ltd. | Refining apparatus and refining method of waste plastic pyrolysis oil |
| US12031097B2 (en) | 2022-10-12 | 2024-07-09 | Ecolab Usa Inc. | Antifouling agents for plastic-derived synthetic feedstocks |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP7130632B2 (en) | Maximizing high-value chemicals from mixed plastics using various steam cracker configurations | |
| US4251500A (en) | Process for hydrocracking a waste rubber | |
| CN105481630B (en) | The method that C-4-fraction selects the butylene of Hydrogenation 1 | |
| CN101616969A (en) | Regenerated rubber and method | |
| DE1026530B (en) | Process for the production of polymers or copolymers of ethylene | |
| JPH0115559B2 (en) | ||
| CN116194555A (en) | Method for treating plastic pyrolysis oil comprising two-step hydrocracking | |
| CA3180070A1 (en) | Process for purifying pyrolized plastic waste | |
| CN101016479A (en) | Method of selective hydrogenation using a catalyst with controlled porosity | |
| EP4281516A1 (en) | Process for hydrodepolymerization of polymeric waste material | |
| RU2272826C1 (en) | Method of processing rubber-containing and other industrial and household organic wastes into chemical raw materials and motor fuel components | |
| US5208404A (en) | Process for producing fuel oil and gas by cracking waste rubber | |
| JPH0948983A (en) | Production of refined oil from decomposed oil of waste plastics | |
| WO1993007105A1 (en) | Conversion of plastic waste to useful oils | |
| CN108624354B (en) | Method for treating organic by-products in cyclohexanone production process | |
| CN114437776B (en) | Method and system for preparing cracking raw material from waste plastic oil and/or waste tire oil | |
| KR20230063995A (en) | Device and method for refining waste plastic pyrolysis oil | |
| US2767160A (en) | Nickel oxide on carbon-alkaline earth hydride catalyst in ethylene polymerization | |
| US2717888A (en) | Nickel oxide and alkali hydride catalyst for ethylene polymerization | |
| JP3617186B2 (en) | How to plasticize oil | |
| JP2024061111A (en) | Method for refining polymer cracked oil and method for producing refined oil | |
| EP1248805A2 (en) | Hydrogenation of hydrocarbon resins | |
| CN114106876A (en) | Catalytic conversion method for producing low-carbon olefin by using chlorine-containing plastic oil | |
| CN105541539A (en) | Method for deolefination non-hydrofining of xylene fraction in reformate | |
| JPH0948981A (en) | Production of refined oil from decomposed oil of waste plastics |