JPH07138576A - Method of processing waste plastic - Google Patents
Method of processing waste plasticInfo
- Publication number
- JPH07138576A JPH07138576A JP5286397A JP28639793A JPH07138576A JP H07138576 A JPH07138576 A JP H07138576A JP 5286397 A JP5286397 A JP 5286397A JP 28639793 A JP28639793 A JP 28639793A JP H07138576 A JPH07138576 A JP H07138576A
- Authority
- JP
- Japan
- Prior art keywords
- hydrogen
- waste plastic
- liquid phase
- oil
- plastic
- 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.)
- Withdrawn
Links
- 229920003023 plastic Polymers 0.000 title claims abstract description 49
- 239000004033 plastic Substances 0.000 title claims abstract description 49
- 239000002699 waste material Substances 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000012545 processing Methods 0.000 title description 3
- 239000002904 solvent Substances 0.000 claims abstract description 36
- 239000007791 liquid phase Substances 0.000 claims abstract description 25
- 239000003054 catalyst Substances 0.000 claims abstract description 7
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 38
- 239000001257 hydrogen Substances 0.000 claims description 38
- 229910052739 hydrogen Inorganic materials 0.000 claims description 38
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 18
- 239000007789 gas Substances 0.000 abstract description 14
- 238000010438 heat treatment Methods 0.000 abstract description 5
- 239000007795 chemical reaction product Substances 0.000 abstract description 2
- 230000000694 effects Effects 0.000 abstract description 2
- 239000007787 solid Substances 0.000 abstract description 2
- 230000001172 regenerating effect Effects 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 24
- 238000005979 thermal decomposition reaction Methods 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 9
- 238000004821 distillation Methods 0.000 description 8
- 239000000126 substance Substances 0.000 description 7
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 238000002474 experimental method Methods 0.000 description 5
- 239000000295 fuel oil Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 229920002635 polyurethane Polymers 0.000 description 4
- 239000004814 polyurethane Substances 0.000 description 4
- 238000000197 pyrolysis Methods 0.000 description 4
- 239000000460 chlorine Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- CXWXQJXEFPUFDZ-UHFFFAOYSA-N tetralin Chemical compound C1=CC=C2CCCCC2=C1 CXWXQJXEFPUFDZ-UHFFFAOYSA-N 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- XECAHXYUAAWDEL-UHFFFAOYSA-N acrylonitrile butadiene styrene Chemical compound C=CC=C.C=CC#N.C=CC1=CC=CC=C1 XECAHXYUAAWDEL-UHFFFAOYSA-N 0.000 description 2
- 229920000122 acrylonitrile butadiene styrene Polymers 0.000 description 2
- 239000004676 acrylonitrile butadiene styrene Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical group 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000010771 distillate fuel oil Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 239000000852 hydrogen donor Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 150000004045 organic chlorine compounds Chemical class 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000013502 plastic waste Substances 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Landscapes
- Processing Of Solid Wastes (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、プラスチック廃棄物を
有効利用するための廃プラスチックの処理方法に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method of treating waste plastic for effectively utilizing plastic waste.
【０００２】[0002]
【従来の技術】産業廃棄物の中で合成の途中又は合成後
の加熱によって軟化し、任意の形に成形できる性質（塑
性）を有するプラスチック類の処理は、従来以下のよう
に行われている。 （１）他の固形廃棄物とともに破砕減容して埋立処分す
る。 （２）熱分解する。 （３）空気により燃焼して廃熱を熱交換器等で回収す
る。2. Description of the Related Art Treatment of plastics which has the property (plasticity) of being industrially softened by heating during synthesis or by heating after synthesis to be molded into an arbitrary shape has been conventionally performed as follows. . (1) Shred and reduce the volume with other solid waste for landfill disposal. (2) Thermal decomposition. (3) Combustion with air to recover waste heat with a heat exchanger or the like.
【０００３】[0003]
【発明が解決しようとする課題】前述した従来の方法に
ついては、各々次のような問題点がある。The above-mentioned conventional methods have the following problems, respectively.
【０００４】（１）埋立処分 有効成分のエネルギ回収がなされず、またプラスチック
は嵩密度が低いため埋立処理の面積が広く必要な上に埋
立場所がなくなりつつあり、腐食分解しないため種々の
公害のもとになる。 （２）熱分解 性質の異なる多数のプラスチックが混在しているので、
熱分解温度が約３００〜８００℃の広範囲になる結果、
低温操作では熱分解残渣が発生し、高温では油の分解や
コーキングトラブルが発生し運転が困難で、生成される
熱分解油は品質が悪く低品質の燃料としてしか使用でき
ないと共に、熱安定性が悪いため、貯蔵時にガム析出等
のトラブルが発生する。また、塩化ビニールを含有する
場合には塩素が油中に含有されるため、更に後処理が必
要となる。 （３）空気による燃焼 プラスチック類は燃焼により約１２００℃以上の高温に
なるため燃焼炉の壁面を損傷しやすく、多量の煤が発生
しサーマルＮＯｘが発生する。また排熱を熱エネルギと
して回収する場合にも、燃焼処理用のプラスチックの供
給量の変動がボイラー負荷に大きく影響し、安定的な操
業が難しい。またプラスチック中に含まれる塩化ビニー
ルや付着する塩類により、排ガス中に有機塩素系の化合
物が含有される場合もあり、その除去対策が不可欠であ
る。(1) Landfill disposal Energy recovery of active ingredients is not performed, and since plastic has a low bulk density, a large area for landfill treatment is required, and the landfill site is disappearing. It becomes the basis. (2) Pyrolysis Since many plastics with different properties are mixed,
As a result of widening the thermal decomposition temperature to about 300-800 ° C,
Pyrolysis residue is generated at low temperature operation, and oil decomposition and coking trouble occur at high temperature and operation is difficult.The pyrolysis oil produced is of poor quality and can only be used as a low-quality fuel, and also has thermal stability. Since it is bad, problems such as gum precipitation occur during storage. Further, when vinyl chloride is contained, chlorine is contained in the oil, so that further post-treatment is required. (3) Combustion with air Since plastics are heated to a high temperature of about 1200 ° C or higher, the wall surface of the combustion furnace is easily damaged, a large amount of soot is generated, and thermal NOx is generated. Also, when exhaust heat is recovered as heat energy, fluctuations in the supply amount of plastic for combustion treatment greatly affect the boiler load, making stable operation difficult. In addition, due to vinyl chloride contained in the plastic and the adhering salts, the exhaust gas may contain an organic chlorine compound, and it is essential to take measures to remove it.
【０００５】一方、従来のプラスチック処理技術とし
て、重油の水添工程にプラスチックを溶解した重油を通
油し水素化分解するもの（Dr.Kunze et al.Sumpfphaseh
ydrierung von Kunststoffen,Teil 2.Kontinuierliche
Versuche.; Praste KautschukVol.40,No.5 Page159,(19
93)参照) がある。この技術は重油の水添工程では触媒
の存在下、重油を水素と反応させるものであるが、プラ
スチックの熱分解反応とそれへの水素添加及び重油への
水素添加が併発する際、軽質な油分への水添が進行しや
すく水素が多量に消費されること、及びプラスチック中
に存在する塩素が水素と反応しＨＣｌを生成する。これ
は触媒と毒となるばかりか反応器材料にとって腐食要因
となるため、特に高温、高圧の水添工程にとっては非常
に好ましくなく、その結果、従来技術は工業化が非常に
難しい困難な技術である。On the other hand, as a conventional plastic processing technique, a method of hydrocracking by passing oil containing heavy oil dissolved in plastic in the hydrogenation process of heavy oil (Dr. Kunze et al. Sumpfphaseh
ydrierung von Kunststoffen, Teil 2.Kontinuierliche
Versuche .; Praste Kautschuk Vol.40, No.5 Page159, (19
See (93)). This technology involves reacting heavy oil with hydrogen in the presence of a catalyst in the hydrogenation process of heavy oil.However, when the thermal decomposition reaction of plastic and hydrogenation of it and hydrogenation of heavy oil occur simultaneously, light oil The hydrogenation to hydrogen is likely to proceed and a large amount of hydrogen is consumed, and chlorine existing in the plastic reacts with hydrogen to generate HCl. This is not only a catalyst and a poison, but also a corrosive factor for the reactor material, and therefore is not very preferable especially for a high temperature and high pressure hydrogenation process, and as a result, the conventional technique is a difficult technique which is very difficult to industrialize. .
【０００６】本発明は、上記従来の問題に対し、廃棄プ
ラスチックのエネルギの有効回収、特に油分を有効に回
収することができる廃プラスチックの処理方法を提供す
ることを目的とする。In order to solve the above-mentioned conventional problems, it is an object of the present invention to provide a method for treating waste plastic, which is capable of effectively recovering energy of waste plastic, particularly oil.
【０００７】[0007]
【課題を解決するための手段】前記目的を達成する本発
明に係る廃プラスチックの処理方法は、廃プラスチック
を水素供与性溶剤の存在下で液相加熱して液相水素化分
解し廃プラスチックを油化する第１工程と、前記工程で
生成した液相留分を触媒の存在下で水添し水素供与性溶
剤を再生する第２工程とからなることを特徴とする。A method for treating waste plastics according to the present invention, which achieves the above object, comprises: heating a waste plastic in a liquid phase in the presence of a hydrogen donating solvent to hydrolyze the waste plastic to decompose the waste plastic. It is characterized by comprising a first step of oiling and a second step of hydrogenating the liquid phase fraction produced in the above step in the presence of a catalyst to regenerate the hydrogen donating solvent.
【０００８】上記構成において、第２工程で生成した水
添油の少なくとも一部を第１工程の水素供与性溶剤とす
ることを特徴とする。In the above structure, at least a part of the hydrogenated oil produced in the second step is used as the hydrogen donating solvent in the first step.
【０００９】上記構成において、廃プラスチックを熱分
解する第１工程の後に、第１工程の熱分解物より液相留
分を分離する工程を設けたことを特徴とする。In the above structure, after the first step of thermally decomposing the waste plastic, a step of separating a liquid phase fraction from the thermally decomposed product of the first step is provided.
【００１０】[0010]
【作用】本発明では、第１工程の液相水素化反応器内に
予め混合スラリー化された水素供与性溶剤と破砕された
廃プラスチックとを供給し、温度４００〜４５０℃、圧
力数十kg／cm2 Ｇ下で約３０分〜３時間反応させる。こ
の操作条件域ではプラスチックは、水素供与性溶剤に溶
解、分離され熱分解ラジカルが発生する。In the present invention, the hydrogen-donating solvent mixed and slurried in advance and the crushed waste plastic are fed into the liquid phase hydrogenation reactor of the first step, and the temperature is 400 to 450 ° C. and the pressure is several tens of kg. / Cm 2 G It is made to react for about 30 minutes to 3 hours. In this operating condition range, the plastic is dissolved and separated in the hydrogen donating solvent to generate a thermal decomposition radical.
【００１１】一方、水素供与性溶剤で溶解される結果、
下式「化１」に示す反応が進行する。On the other hand, as a result of being dissolved in a hydrogen donating solvent,
The reaction represented by the following formula "Chemical formula 1" proceeds.
【化１】 [Chemical 1]
【００１２】すなわち、プラスチックが熱分解してモノ
マー化する際に生成するラジカルがＨ・と反応する結
果、軽質で安定な油分が生成することとなる。またその
際熱分解ガス、軟質炭化水素ガスが一部生成し、プラス
チック中に塩化ビニールなどの塩素化合物がある際に
は、塩化水素（ＨＣｌ）ガスとして大部分が除去され
る。That is, as a result of the radicals generated when the plastic is thermally decomposed and converted into a monomer to react with H., a light and stable oil component is generated. At that time, pyrolysis gas and soft hydrocarbon gas are partially generated, and when chlorine compounds such as vinyl chloride are present in the plastic, most of them are removed as hydrogen chloride (HCl) gas.
【００１３】本プロセスでは、第１工程で廃プラスチッ
クを液相化し、前記工程で生成した液相分と水素とを水
添触媒反応器へ送り、４００〜４５０℃、圧力１００〜
１５０kg／cm2 Ｇの条件下で第２工程の水添反応を行
い、油相分中の溶剤を再生反応させることができる。こ
の第２工程の生成物は、蒸留器により水素供与性溶剤留
分を分離回収し、水素供与性溶剤は再び液化反応器へ循
環供給し、第１工程において再び利用する。また水素供
与性溶剤の留分以外は生成物として系外へ取出し、製品
油として使用できる。In this process, the waste plastic is liquefied in the first step, the liquid phase component produced in the above step and hydrogen are sent to the hydrogenation catalytic reactor, and the temperature is 400 to 450 ° C. and the pressure is 100 to 450 ° C.
The hydrogenation reaction in the second step can be carried out under the condition of 150 kg / cm 2 G to regenerate the solvent in the oil phase. In the product of the second step, a hydrogen donating solvent fraction is separated and recovered by a distiller, and the hydrogen donating solvent is circulated again to the liquefaction reactor and reused in the first step. Further, except for the hydrogen-donating solvent fraction, it can be taken out of the system as a product and used as a product oil.
【００１４】[0014]
【実施例】以下、本発明を図に示す実施例について詳細
に説明する。図１は本発明の工程を示すブロック図であ
る。図において、１は廃プラスチック、２は循環水素供
与性溶剤、３は水素供給源、４は水素供与性溶剤源、５
はガス、６は回収される油、７は残渣、１０は液化反応
器（第１工程）、１１は分離器、１２は水添反応器（第
２工程）、１３は蒸留塔、１４は蒸留塔１３から液化反
応器１０入口へ接続した循環管、１５は水素供給管、１
６は水素供与性溶剤補充管、１７はガス排出管、１８は
残渣回収管である。Embodiments of the present invention will be described below in detail with reference to the drawings. FIG. 1 is a block diagram showing the steps of the present invention. In the figure, 1 is waste plastic, 2 is a circulating hydrogen donating solvent, 3 is a hydrogen source, 4 is a hydrogen donating solvent source, 5
Is a gas, 6 is an oil to be recovered, 7 is a residue, 10 is a liquefaction reactor (first step), 11 is a separator, 12 is a hydrogenation reactor (second step), 13 is a distillation column, and 14 is distillation. A circulation pipe connected from the tower 13 to the inlet of the liquefaction reactor 10, 15 is a hydrogen supply pipe, 1
6 is a hydrogen donating solvent replenishment pipe, 17 is a gas discharge pipe, and 18 is a residue recovery pipe.
【００１５】本実施例においては、廃プラスチック１を
水素供与性溶剤２の存在下で液相加熱してプラスチック
を液相水素化分解し、軽質な油分と副生気体を生成させ
る第１工程と、これに引続き気体及び固体を分離器１１
を用いて液相留分１９と分離する分離工程と、前記工程
で生成した液相留分１９を触媒の存在下で水素と反応さ
せ、水素供与性溶剤を再生する第２工程とによる２段階
でプラスチックを油化するものである。尚、分離工程を
第１工程又は第２工程のいずれかに含めるようにしても
よい。In the present embodiment, the waste plastic 1 is subjected to liquid phase heating in the presence of the hydrogen donating solvent 2 to perform liquid phase hydrocracking of the plastic to produce a light oil and a by-product gas. , Followed by gas and solids separator 11
In a second step in which the liquid-phase fraction 19 produced in the above step is reacted with hydrogen in the presence of a catalyst to regenerate the hydrogen-donating solvent. It is an oil that plasticizes. The separation step may be included in either the first step or the second step.
【００１６】以下、処理方法について説明する。第１工
程の液化反応器１０内に、水素供与性溶剤２と細かく破
砕された廃プラスチック１とを一定の割合で混合スラリ
ー化して供給し、一定の温度、圧力、時間下で反応させ
ると、液相化したプラスチック１と水素供与性溶剤２と
の接触反応で下記「化２」に示す水素移行反応が生成し
て、プラスチック１の成分がガス５と油６と残渣７とに
分解される。ここで、廃プラスチック１と水素供与性溶
剤２とをスラリー化する混合槽を設けても何ら差支えな
い。次いで、液化反応器１０内の生成物を分離器１１へ
送り、ガス５及び残渣７を分離し、液相留分１９を第２
工程の水添反応器１２に供給する。The processing method will be described below. In the liquefaction reactor 10 of the first step, the hydrogen donating solvent 2 and the finely crushed waste plastic 1 are mixed and slurried at a constant ratio and supplied, and reacted at a constant temperature, pressure and time, The hydrogen transfer reaction shown in the following "Chemical formula 2" is generated by the contact reaction between the liquid phase plastic 1 and the hydrogen donating solvent 2, and the components of the plastic 1 are decomposed into gas 5, oil 6 and residue 7. . Here, there is no problem even if a mixing tank for slurrying the waste plastic 1 and the hydrogen donating solvent 2 is provided. Next, the product in the liquefaction reactor 10 is sent to the separator 11, the gas 5 and the residue 7 are separated, and the liquid phase fraction 19 is separated into the second fraction.
It is supplied to the hydrogenation reactor 12 of the process.
【化２】 [Chemical 2]
【００１７】第２工程の水添反応器１２には、水素ガス
と必要に応じて補充の水素供与性溶剤が供給され、一定
の温度、圧力、時間下で反応させると、第１工程から送
られ、分離器１１を介して分離された液相留分と水素と
の接触水素化反応で、下記「化３」に示す水素化反応が
生起し、液相留分中の溶剤成分が水素供与性溶剤２に再
生される。The hydrogenation reactor 12 in the second step is supplied with hydrogen gas and, if necessary, supplemental hydrogen donating solvent, and when the reaction is carried out at a constant temperature, pressure and time, the hydrogen is fed from the first step. The hydrogenation reaction shown in the following "Chemical Formula 3" occurs in the catalytic hydrogenation reaction between the liquid phase fraction separated through the separator 11 and hydrogen, and the solvent component in the liquid phase fraction contributes hydrogen. It is regenerated into the organic solvent 2.
【化３】 [Chemical 3]
【００１８】尚、上記「化３」において水素供与性溶剤
としてアントラセンを例示したが、何らアントラセンに
限定されることなく２環以上の芳香族系炭化水素でその
化合物が水素供与性を示すもので常温〜０℃で液状であ
れば、如何なるものでも使用可能である。水添反応器１
２で生成した反応物を蒸留塔１３へ送り蒸留し、水素供
与性溶剤２の留分を分留後循環管１４を経由し液化反応
器１０の入り側へ循環供給する。In the above "Chemical Formula 3", anthracene was exemplified as the hydrogen donating solvent, but the compound is not limited to anthracene, but is an aromatic hydrocarbon having two or more rings, and the compound exhibits a hydrogen donating property. Any material can be used as long as it is liquid at room temperature to 0 ° C. Hydrogenation reactor 1
The reaction product generated in 2 is sent to the distillation column 13 for distillation, and the fraction of the hydrogen donating solvent 2 is fractionally distilled and then circulated and supplied to the inlet side of the liquefaction reactor 10 via the circulation pipe 14.
【００１９】同時に、蒸留塔１３の塔頂からはガス５
が、また塔底からはサイドカット留分としてプラスチッ
クからの生成油が回収される。At the same time, gas 5 flows from the top of the distillation column 13.
However, the produced oil from the plastic is recovered as a side cut fraction from the tower bottom.
【００２０】次に図２は、上述した本発明による廃プラ
スチック１の液化処理において、供試材としてＡＢＳ
（アクリロニトリルブタジエンスチレン）とテトラリン
とを使用し、温度、時間圧力、溶剤量を変更して行った
三つの第１工程反応による液相水素化実験の例（テスト
No. Ａ−１，Ａ−２，Ａ−３）と、従来の熱分解による
実験例（Ａ−４）の結果の比較を示す。Next, FIG. 2 shows ABS as a test material in the liquefaction treatment of the waste plastic 1 according to the present invention described above.
(Acrylonitrile butadiene styrene) and tetralin using liquid phase hydrogenation experiment by three first step reactions performed by changing temperature, time pressure and solvent amount (test
The results of No. A-1, A-2, A-3) and the experimental example (A-4) by the conventional thermal decomposition are compared.
【００２１】[0021]
【表１】 表１は、図２及び後述する図４の本発明の実験に使用し
た廃プラスチックの分析表である。[Table 1] Table 1 is an analysis table of the waste plastic used in the experiment of the present invention in FIG. 2 and FIG. 4 described later.
【００２２】図２の実験例（Ａ−１）は、温度４００
℃、処理時間０．５時間、初期圧力５kg／cm2 Ｇ、溶剤
／プラスチック重量比＝３、の条件下で第１工程反応を
行った。実験例（Ａ−２）は、上記実験例（Ａ−１）の
処理時間だけを１時間に変更した条件下での第１工程反
応を行った。実験例（Ａ−３）は、上記実験例（Ａ−
２）の温度を４５０℃、初期圧力を２kg／cm2 Ｇ、溶剤
量を溶剤／プラスチック重量比＝２、に変更した条件下
での第１工程反応を行った。比較例（Ａ−４）は、前記
実験例（Ａ−３）と略同一条件下で溶剤なしに行った熱
分解反応である。The experimental example (A-1) in FIG.
The first step reaction was carried out under conditions of a temperature of 0.5 ° C., a treatment time of 0.5 hours, an initial pressure of 5 kg / cm 2 G and a solvent / plastic weight ratio = 3. In Experimental Example (A-2), the first step reaction was carried out under the condition that only the treatment time of Experimental Example (A-1) was changed to 1 hour. The experimental example (A-3) is the same as the experimental example (A-
The first step reaction was carried out under the conditions that the temperature of 2) was changed to 450 ° C., the initial pressure was changed to 2 kg / cm 2 G, and the amount of solvent was changed to solvent / plastic weight ratio = 2. Comparative Example (A-4) is a thermal decomposition reaction carried out under the same conditions as in Experimental Example (A-3) above without using a solvent.
【００２３】図２に示される結果から、本発明による実
験例（Ａ−１）〜（Ａ−３）の油生成率が、従来の熱分
解による比較例（Ａ−４）に比較し、著しく優れること
が明瞭である。From the results shown in FIG. 2, the oil production rates of Experimental Examples (A-1) to (A-3) according to the present invention are significantly higher than those of the conventional Comparative Example (A-4) by thermal decomposition. It is clearly superior.
【００２４】また、図３は、図２の実験結果で得られた
油生成の蒸留性状を示したものである。図３に示される
ように、従来の熱分解による比較例（Ａ−４）で得られ
る油は、低沸点から高沸点までの留分の混合物である。
一方、本発明の実験例（Ａ−１）〜（Ａ−３）では反応
温度、時間に比例して軽質化が進行し、（Ａ−３）の生
成油では１ＢＰ１００℃〜ＥＰ４２０℃の油が取得され
ている。FIG. 3 shows the distillation characteristics of oil production obtained from the experimental results of FIG. As shown in FIG. 3, the oil obtained in Comparative Example (A-4) by conventional thermal decomposition is a mixture of fractions having a low boiling point to a high boiling point.
On the other hand, in Experimental Examples (A-1) to (A-3) of the present invention, lightening progresses in proportion to the reaction temperature and time, and in the produced oil of (A-3), oil of 1BP100 ° C to EP420 ° C is produced. Has been acquired.
【００２５】次に、図４は、前記図２で行った実験例
（Ａ−２）と、略同一の処理条件のもとで、塩化ビニル
（ＰＶＣ）及びポリウレタン（ＰＵＲ）を供試材として
行った本発明の第１工程反応による液相水素化の実験例
（Ｖ−１）（Ｕ−１）の実験結果の比較を示す。Next, FIG. 4 shows vinyl chloride (PVC) and polyurethane (PUR) as test materials under substantially the same processing conditions as the experimental example (A-2) performed in FIG. The comparison of the experiment result of the experiment example (V-1) (U-1) of the liquid phase hydrogenation by the 1st process reaction of this invention performed is shown.
【００２６】図４に示されるように、塩化ビニル（ＰＶ
Ｃ）及びポリウレタン（ＰＵＲ）においても、図２の熱
分解による従来型の実験例（Ａ−４）に比較すると、優
れた油生成率を得ることが明らかである。As shown in FIG. 4, vinyl chloride (PV
It is clear that even in C) and polyurethane (PUR), an excellent oil production rate is obtained as compared with the conventional experimental example (A-4) by thermal decomposition in FIG.
【００２７】[0027]
【発明の効果】以上要するに、本発明は、廃プラスチッ
クを水素供与性溶剤の存在下で液相水素化分解し廃プラ
スチックを油化する第１工程と、前記工程で生成した液
相分を触媒の存在化で水素ガスと反応させ水添軽質化す
る第２工程により液化処理することによって、産業廃棄
物としてのプラスチック類から軽質の燃料油を高い油生
成率で回収し有効利用することを可能にした効果を奏し
たものである。In summary, according to the present invention, the first step of liquid phase hydrocracking waste plastic in the presence of a hydrogen donating solvent to oilize the waste plastic, and the liquid phase component produced in the above step are used as a catalyst. It is possible to recover light fuel oil from plastics as industrial waste at a high oil production rate and use it effectively by performing a liquefaction process in the second step of reacting with hydrogen gas and hydrogenating and lightening it in the presence of hydrogen. It has the effect of
【図１】本発明に係る廃プラスチック処理方法の実験例
の工程を示すブロック図である。FIG. 1 is a block diagram showing steps of an experimental example of a waste plastic treatment method according to the present invention.
【図２】本発明による３つの実験例と従来の熱分解の実
験例の結果の比較図である。FIG. 2 is a comparison diagram of the results of three experimental examples according to the present invention and a conventional thermal decomposition experimental example.
【図３】図２により生成した油の蒸留性状の比較図であ
る。FIG. 3 is a comparison diagram of distillation properties of the oil produced according to FIG.
【図４】種類の異なる３種の廃プラスチックについて行
なった本発明の実験結果を示す図である。FIG. 4 is a diagram showing the results of experiments of the present invention performed on three types of waste plastics of different types.
１ 廃プラスチック ２ 水素供与性溶剤 ３ 水素供給源 ４ 水素供与性溶剤供給源 ５ ガス ６ 油 ７ 残渣 １０ 液化反応器（第１工程） １１ 分離器 １２ 水添反応器（第２工程） １３ 蒸留塔 １４ 循環管 １５ 水素供給管 １６ 水素供与性溶剤補充管 １７ ガス排出管 １８ 残渣回収管 １９ 液相留分 1 Waste plastic 2 Hydrogen donating solvent 3 Hydrogen source 4 Hydrogen donating solvent source 5 Gas 6 Oil 7 Residue 10 Liquefaction reactor (first step) 11 Separator 12 Hydrogenation reactor (second step) 13 Distillation column 14 Circulation Pipe 15 Hydrogen Supply Pipe 16 Hydrogen Donor Solvent Replenishment Pipe 17 Gas Discharge Pipe 18 Residue Recovery Pipe 19 Liquid Phase Fraction
───────────────────────────────────────────────────── 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 // Ｃ０７Ｂ 61/00 ３００ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification number Office reference number FI technical display location // C07B 61/00 300
Claims (3)
下で液相加熱して液相水素化分解し廃プラスチックを油
化する第１工程と、前記工程で生成した液相分を触媒の
存在下で水添し水素供与性溶剤を再生する第２工程とか
らなることを特徴とする廃プラスチックの処理方法。1. A first step in which waste plastic is liquid-phase heated in the presence of a hydrogen-donating solvent to perform liquid-phase hydrocracking to oilize the waste plastic, and a liquid phase component produced in the step is present in the presence of a catalyst. A second step of hydrogenating below to regenerate the hydrogen donating solvent.
水添油の少なくとも一部を第１工程の水素供与性溶剤と
することを特徴とする廃プラスチックの処理方法。2. The method for treating waste plastic according to claim 1, wherein at least a part of the hydrogenated oil produced in the second step is used as the hydrogen donating solvent in the first step.
分解する第１工程の後に、第１工程の熱分解物より液相
留分を分離する工程を設けたことを特徴とする廃プラス
チックの処理方法。3. The treatment of waste plastic according to claim 1, further comprising a step of separating a liquid phase fraction from the pyrolyzate of the first step after the first step of thermally decomposing the waste plastic. Method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5286397A JPH07138576A (en) | 1993-11-16 | 1993-11-16 | Method of processing waste plastic |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5286397A JPH07138576A (en) | 1993-11-16 | 1993-11-16 | Method of processing waste plastic |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH07138576A true JPH07138576A (en) | 1995-05-30 |
Family
ID=17703879
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5286397A Withdrawn JPH07138576A (en) | 1993-11-16 | 1993-11-16 | Method of processing waste plastic |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH07138576A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6162894A (en) * | 1998-07-28 | 2000-12-19 | Director-General Of Agency Of Industrial Science And Technology | Method of treating resin materials to yield oils |
| WO2023279019A1 (en) * | 2021-06-29 | 2023-01-05 | Sabic Global Technologies B.V. | Systems and methods for processing mixed plastic waste |
| CN116355643A (en) * | 2021-12-29 | 2023-06-30 | 深圳世纪星源股份有限公司 | Method for hydrothermally treating polyolefin plastics |
-
1993
- 1993-11-16 JP JP5286397A patent/JPH07138576A/en not_active Withdrawn
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6162894A (en) * | 1998-07-28 | 2000-12-19 | Director-General Of Agency Of Industrial Science And Technology | Method of treating resin materials to yield oils |
| WO2023279019A1 (en) * | 2021-06-29 | 2023-01-05 | Sabic Global Technologies B.V. | Systems and methods for processing mixed plastic waste |
| CN116355643A (en) * | 2021-12-29 | 2023-06-30 | 深圳世纪星源股份有限公司 | Method for hydrothermally treating polyolefin plastics |
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