JPH07102264A - Equipment for producing oil from waste plastic - Google Patents
Equipment for producing oil from waste plasticInfo
- Publication number
- JPH07102264A JPH07102264A JP24542593A JP24542593A JPH07102264A JP H07102264 A JPH07102264 A JP H07102264A JP 24542593 A JP24542593 A JP 24542593A JP 24542593 A JP24542593 A JP 24542593A JP H07102264 A JPH07102264 A JP H07102264A
- Authority
- JP
- Japan
- Prior art keywords
- raw material
- tank
- material mixing
- oil
- thermal decomposition
- 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
Links
- 229920003023 plastic Polymers 0.000 title claims abstract description 60
- 239000004033 plastic Substances 0.000 title claims abstract description 60
- 239000002699 waste material Substances 0.000 title claims abstract description 49
- 239000002994 raw material Substances 0.000 claims abstract description 71
- 238000002156 mixing Methods 0.000 claims abstract description 53
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 28
- 238000005979 thermal decomposition reaction Methods 0.000 claims abstract description 27
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 24
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000003421 catalytic decomposition reaction Methods 0.000 claims abstract description 5
- 238000003756 stirring Methods 0.000 claims abstract description 5
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000000463 material Substances 0.000 abstract description 14
- 239000007789 gas Substances 0.000 abstract description 9
- 230000007797 corrosion Effects 0.000 abstract description 5
- 238000005260 corrosion Methods 0.000 abstract description 5
- 238000005406 washing Methods 0.000 abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 5
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000000155 melt Substances 0.000 abstract description 4
- 238000000354 decomposition reaction Methods 0.000 abstract description 3
- 238000013019 agitation Methods 0.000 abstract 2
- 238000009434 installation Methods 0.000 abstract 2
- 238000002844 melting Methods 0.000 description 16
- 230000008018 melting Effects 0.000 description 16
- 238000000034 method Methods 0.000 description 14
- 238000000197 pyrolysis Methods 0.000 description 9
- 238000010586 diagram Methods 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 3
- 238000004523 catalytic cracking Methods 0.000 description 3
- 238000006298 dechlorination reaction Methods 0.000 description 3
- 238000007033 dehydrochlorination reaction Methods 0.000 description 3
- 230000006866 deterioration Effects 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 230000004323 axial length Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229910000856 hastalloy Inorganic materials 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
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
- 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
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Processing Of Solid Wastes (AREA)
- Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、廃プラスチック材を溶
融・分解して、低分子炭化水素化合物を得る廃プラスチ
ック処理設備における廃プラスチックの溶融方法に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method of melting waste plastic in a waste plastic processing facility for melting and decomposing waste plastic material to obtain a low molecular weight hydrocarbon compound.
【０００２】[0002]
【従来の技術】従来、廃プラスチック材の溶融加熱分解
手段として、例えば、特公平３−８６７９１号公報に記
載された方式のものがある。2. Description of the Related Art Conventionally, as a means for melting and decomposing waste plastic materials, there is, for example, a method disclosed in Japanese Patent Publication No. 3-86791.
【０００３】この方式は、図７に示すように、破砕装置
によって得た廃プラスチック破砕物Ａを押出機（ルー
ダ）１によって加熱・混錬して一次溶融したのち、原料
混合槽２に供給し、この原料混合槽で二次溶融・分解し
て一次溶融物Ｂを熱分解槽３に供給し、この溶融物の気
化物を接触分解槽４において低分子炭化水素化合物に接
触転化するものである。In this system, as shown in FIG. 7, a waste plastic crushed material A obtained by a crusher is heated and kneaded by an extruder (ruder) 1 to be primarily melted, and then supplied to a raw material mixing tank 2. The secondary melting / decomposition in this raw material mixing tank, the primary melt B is supplied to the thermal decomposition tank 3, and the vaporized product of this melt is catalytically converted into a low molecular weight hydrocarbon compound in the catalytic cracking tank 4. .
【０００４】このように、この従来の方式における熱分
解槽３に供給されるプラスチック材は、一旦、押出機
（ルーダ）１によって一次溶融されたのち原料混合槽２
において二次溶融・分解して、この原材料を熱分解槽３
に均一な溶融・分解状態で供給して、安定した熱分解プ
ロセスを達成しようとするものである。As described above, the plastic material supplied to the thermal decomposition tank 3 in this conventional system is once melted by the extruder (ruder) 1 and then the raw material mixing tank 2 is used.
Secondly melted and decomposed in the
It is intended to achieve a stable thermal decomposition process by supplying the same in a uniformly melted and decomposed state.
【０００５】[0005]
【発明が解決しようとする課題】しかしながら、廃プラ
スチック材の中に塩化ビニルを多く含有する場合には、
この押出機において、多量の塩化水素ガスが発生し、原
材料に含まれる水分の共存下で該押出機の低温部にて塩
化水素ガスが凝縮して塩酸となるため、ハステロイなど
の高価な耐腐食材料を適用する必要があり、高価なもの
とならざるを得ない。However, when a large amount of vinyl chloride is contained in the waste plastic material,
In this extruder, a large amount of hydrogen chloride gas is generated, and in the coexistence of water contained in the raw material, the hydrogen chloride gas condenses into hydrochloric acid in the low temperature part of the extruder, resulting in expensive corrosion resistance such as Hastelloy. Materials have to be applied, which is expensive.
【０００６】また、製品油への塩化水素の混入による油
品質の劣化を防止するためには、前段である押出機に
て、発生する多量の塩化水素ガスを押出機内から外部へ
吸引等で完全に除去する必要があり、そのためには、押
出機の軸方向の長さを極端に長くし、押出機内で一次溶
融された廃プラスチック材を長時間にわたって攪拌・滞
流しなければならず、押出機の設備費が極端にアップす
ると共に廃プラスチック処理設備全体として連続処理を
行う中、前記押出機での長時間の攪拌・滞流時間は円滑
なる連続処理を阻害する。このため、従来、押出機の軸
方向の長さは、生産性を重視した連続処理を円滑に行え
るよう適度な軸方向長さとしている。Further, in order to prevent deterioration of oil quality due to mixing of hydrogen chloride into product oil, a large amount of generated hydrogen chloride gas is completely sucked from the inside of the extruder to the outside in the extruder in the preceding stage. In order to do so, the length of the extruder in the axial direction must be made extremely long, and the waste plastic material that has been primarily melted in the extruder must be agitated and stagnant for a long time. While the equipment cost of (1) is extremely increased and the continuous processing is performed as the entire waste plastic processing equipment, a long stirring and stagnant time in the extruder hinders smooth continuous processing. For this reason, conventionally, the axial length of the extruder is set to an appropriate axial length so that continuous processing with an emphasis on productivity can be smoothly performed.
【０００７】それにより押出機以降の例えば原料混合
槽、熱分解槽において溶融プラスチック中から塩化水素
が発生し、これが製品の油の中へ混入するため、例えば
脱クロル槽等の脱クロル手段が必要であった。As a result, hydrogen chloride is generated from the molten plastic in, for example, the raw material mixing tank and the thermal decomposition tank after the extruder, and this is mixed into the oil of the product. Therefore, dechlorination means such as a dechlorination tank is required. Met.
【０００８】また、廃プラスチック材を押出機において
溶融・混錬するには押出機内で溶融する廃プラスチック
材の粘性が高いため、多大の駆動力を要する。Further, in order to melt and knead the waste plastic material in the extruder, a large driving force is required because the viscosity of the waste plastic material melted in the extruder is high.
【０００９】このように従来の押出機においては、前記
のとおり、 塩化水素に耐える高価な耐腐食材料にて押出機を製
作しなければならない。As described above, in the conventional extruder, the extruder must be made of an expensive corrosion-resistant material that can withstand hydrogen chloride.
【００１０】 押出機の後流側の設備に別に脱クロル
手段が必要。Separate dechlorination means is required for equipment on the downstream side of the extruder.
【００１１】 操業時に多大の電力を必要とする。A large amount of electric power is required during operation.
【００１２】等の種々の課題がある。There are various problems such as
【００１３】したがって、押出機によるこの一次溶融を
省略できれば、廃プラスチック処理設備全体としての設
備費用・操業費用の低減のみならず、建設工程も短縮で
き、利点は多大なものである。Therefore, if the primary melting by the extruder can be omitted, not only the facility cost and operating cost of the entire waste plastic processing facility can be reduced, but also the construction process can be shortened, which is a great advantage.
【００１４】ところが、この押出機を単に省略しただけ
では、原料混合槽内に常温で投入される廃プラスチック
破砕物Ａと熱分解槽から供給される液状のプラスチック
溶融物との混合が十分に行われず、その均一溶融物を得
るのに時間と手間を要し、生産性及び油品質の低下をま
ねくと共に、塩化ビニルの加熱による塩化水素ガスの多
量の発生による設備への耐腐食対策を施す必要があり、
設備費用面で、押出機を設けた従来のものよりも逆に高
価なものとならざるを得ない。However, by simply omitting this extruder, the waste plastic crushed material A, which is charged into the raw material mixing tank at room temperature, and the liquid plastic melt supplied from the thermal decomposition tank are sufficiently mixed. In addition, it takes time and labor to obtain a homogeneous melt, which leads to deterioration of productivity and oil quality, and it is necessary to take measures against corrosion to equipment due to the generation of a large amount of hydrogen chloride gas by heating vinyl chloride. There is
In terms of equipment cost, it is inevitably more expensive than the conventional one equipped with an extruder.
【００１５】本発明の目的は、原料廃プラスチック材の
溶融・分解による低分子炭化水素化合物化における原料
の溶融・分解・油化処理において、押出機のような一次
溶融装置を使用することなく、また、廃プラスチック処
理設備全体の連続操業を円滑に行うとともに油品質の低
下を起こすことなく、更に原材料中の塩化ビニルの分解
により発生する塩化水素ガスの凝縮による塩酸腐食被害
の発生がない手段を提供することにある。An object of the present invention is to melt, decompose, and oilize a raw material in a low molecular weight hydrocarbon compound by melting and decomposing a waste plastic material without using a primary melting device such as an extruder. In addition, a means for smooth continuous operation of the entire waste plastic processing facility, without causing deterioration of oil quality, and without causing hydrochloric acid corrosion damage due to condensation of hydrogen chloride gas generated by the decomposition of vinyl chloride in the raw material. To provide.
【００１６】[0016]
【課題を解決するための手段】前記の課題を解決するた
めに、本発明の廃プラスチックの油化製造設備は、上部
に廃プラスチックの投入口を有する少なくとも２個以上
の原料混合槽を配設し、該原料混合槽の後流側に熱分解
槽及び接触分解槽を直列に連設し、前記熱分解槽と前記
複数の原料混合槽とを両者の内容物を循環せしめるよう
に接続し、前記原料混合槽に内容物の攪拌手段およびま
たは自己循環手段を設けるとともに塩化水素の除去手段
を配設してなることを特徴とする。In order to solve the above-mentioned problems, in the waste plastic oil production facility of the present invention, at least two or more raw material mixing tanks each having a waste plastic inlet are provided in the upper part. Then, a thermal decomposition tank and a catalytic decomposition tank are connected in series on the downstream side of the raw material mixing tank, and the thermal decomposition tank and the plurality of raw material mixing tanks are connected so as to circulate the contents of both. The raw material mixing tank is provided with a stirring means for contents and / or a self-circulating means and a means for removing hydrogen chloride.
【００１７】[0017]
【作用】複数の原料混合槽Ａ、Ｂにより、交互に廃プラ
スチック原料を処理し、熱分解槽へ連続して供給するた
め結果的には、廃プラスチックの油化製造設備全体とし
て、連続して処理できる。The waste plastic raw materials are alternately processed by the plurality of raw material mixing tanks A and B and continuously supplied to the thermal decomposition tank. As a result, the waste plastic oil production facility as a whole is continuously supplied. It can be processed.
【００１８】原料混合槽において、廃プラスチック原料
に含まれている特に塩化水素等を完全に除去することが
できる。In the raw material mixing tank, particularly hydrogen chloride and the like contained in the waste plastic raw material can be completely removed.
【００１９】以上により押出機を省略することができ
る。As described above, the extruder can be omitted.
【００２０】[0020]
【実施例】図１に、本発明の廃プラスチックの油化処理
設備の全体概要図を示す。EXAMPLE FIG. 1 shows an overall schematic diagram of an oil treatment equipment for waste plastics according to the present invention.
【００２１】図中、２は原料混合槽、３は熱分解槽、４
は接触分解槽、５はポンプ、６はバルブ、７は排風機、
８は塩化水素の除去手段である水洗塔、９は原料混合槽
への廃プラスチック原料の投入口、１０は攪拌手段であ
る回転式攪拌機、１２は原料混合槽内での溶融ポンプに
よる自己循環手段を示す。In the figure, 2 is a raw material mixing tank, 3 is a thermal decomposition tank, 4
Is a catalytic cracking tank, 5 is a pump, 6 is a valve, 7 is a blower,
8 is a water washing tower which is a means for removing hydrogen chloride, 9 is an inlet of the waste plastic raw material to the raw material mixing tank, 10 is a rotary stirrer which is a stirring means, 12 is a self-circulating means by a melting pump in the raw material mixing tank Indicates.
【００２２】以上の主な各部品より、本発明の廃プラス
チックの油化処理設備が構成される。The above-mentioned main parts constitute the waste plastic oil treatment equipment of the present invention.
【００２３】図２〜図５を用いて、本発明の廃プラスチ
ックの油化処理設備を使用した廃プラスチックの油化処
理方法を説明する。2 to 5, the method for oil treatment of waste plastic using the oil treatment equipment for waste plastic of the present invention will be described.
【００２４】なお、図２〜図５において、バルブ６の開
閉状態については、◇を開、◆を閉として各図共通で表
す。In FIGS. 2 to 5, the open / closed state of the valve 6 is shown in common in each figure, with ⋄ open and ♦ closed.
【００２５】＜工程１＞図２を参照して、予め破砕機等
により切断・破砕された廃プラスチックの原料を原料混
合槽Ａに、廃プラスチック原料の投入口９を開口して内
部に投入し、その後、該投入口９を閉める。つぎに熱分
解槽４から約４００〜４５０℃の熱分解油を原料混合槽
Ａに搬入する。<Step 1> Referring to FIG. 2, the raw material of the waste plastic that has been cut and crushed by a crusher or the like in advance is introduced into the raw material mixing tank A by opening the injection port 9 for the waste plastic material. Then, the charging port 9 is closed. Next, the pyrolysis oil at about 400 to 450 ° C. is carried into the raw material mixing tank A from the pyrolysis tank 4.
【００２６】原料混合槽Ａでは、投入した廃プラスチッ
クの原料が、熱分解槽４から供給される約４００〜４５
０℃の熱分解油により溶融されていくが、この時、溶融
促進、溶融プラスチック表面更新のために、回転式攪拌
機１０を回転または原料混合槽Ａ内の溶融物を自己循環
手段により循環させる。In the raw material mixing tank A, the raw material of the waste plastic that has been input is supplied from the thermal decomposition tank 4 to about 400 to 45.
It is melted by the pyrolysis oil at 0 ° C. At this time, the rotary stirrer 10 is rotated or the melt in the raw material mixing tank A is circulated by the self-circulation means in order to accelerate melting and renew the surface of the molten plastic.
【００２７】原料混合槽Ａでの溶融・反応温度は、約２
５０〜３５０℃であり、従って、投入した廃プラスチッ
クの原料にＰＶＣの混入がない場合には、約１時間以
上、またＰＶＣが混入する場合には、約３〜５時間以上
この温度状態を保持し、投入した廃プラスチック原料に
含まれている特に塩化水素を全て離脱させる。離脱した
塩化水素は、水洗塔に送られ無害化され、その後大気中
に放散される。The melting / reaction temperature in the raw material mixing tank A is about 2
50 to 350 ° C. Therefore, when PVC is not mixed in the input waste plastic raw material, this temperature state is maintained for about 1 hour or more, and when PVC is mixed, for about 3 to 5 hours or more. Then, in particular, all hydrogen chloride contained in the input waste plastic raw material is released. The released hydrogen chloride is sent to a washing tower to be harmless, and then released into the atmosphere.
【００２８】＜工程２＞図３を参照して、一方、前記の
処理の間、好ましくは原料混合槽Ａでの必要な溶融・混
合時間の約半分経過後に、原料混合槽Ｂにおいては、前
記原料混合槽Ａと同じ処理をする。<Step 2> Referring to FIG. 3, on the other hand, in the raw material mixing tank B, preferably about half of the required melting / mixing time in the raw material mixing tank A has elapsed during the above treatment. The same process as the raw material mixing tank A is performed.
【００２９】詳しく説明すると、予め破砕機等により切
断・破砕された廃プラスチックの原料を原料混合槽Ｂ
に、廃プラスチック原料の投入口９を開口し内部に投入
し、その後該投入口９を閉める。つぎに熱分解槽４から
約４００〜４５０℃の熱分解油を原料混合槽Ｂに搬入す
る。More specifically, waste plastic raw materials that have been cut and crushed by a crusher or the like in advance are used as a raw material mixing tank B.
Then, the input port 9 for the waste plastic raw material is opened and charged into the inside, and then the input port 9 is closed. Next, the pyrolysis oil at about 400 to 450 ° C. is carried into the raw material mixing tank B from the pyrolysis tank 4.
【００３０】原料混合槽Ｂでは、投入した廃プラスチッ
クの原料が、熱分解槽４から供給される約３５０〜４０
０℃の熱分解油により溶融されていくが、この時、溶融
促進、溶融プラスチックの表面更新のために、回転式攪
拌機１０を回転または原料混合槽Ｂ内の溶融物を自己循
環手段により循環させる。In the raw material mixing tank B, about 350 to 40 raw material of the waste plastic that is input is supplied from the thermal decomposition tank 4.
It is melted by pyrolysis oil at 0 ° C. At this time, the rotary stirrer 10 is rotated or the melt in the raw material mixing tank B is circulated by the self-circulation means in order to accelerate melting and renew the surface of the molten plastic. .
【００３１】原料混合槽Ｂでの溶融・反応温度は、約２
５０〜３５０℃であり、従って、投入した廃プラスチッ
クの原料にＰＶＣの混入がない場合には、約１時間以
上、またＰＶＣが混入する場合には、約３〜５時間以上
この温度状態を保持し、投入した廃プラスチック原料に
含まれている特に塩化水素を全て離脱させる。The melting / reaction temperature in the raw material mixing tank B is about 2
50 to 350 ° C. Therefore, when PVC is not mixed in the input waste plastic raw material, this temperature state is maintained for about 1 hour or more, and when PVC is mixed, for about 3 to 5 hours or more. Then, in particular, all hydrogen chloride contained in the input waste plastic raw material is released.
【００３２】離脱した塩化水素は、水洗塔に送られて無
害化され、その後大気中に放散される。The desorbed hydrogen chloride is sent to a water washing tower to be rendered harmless, and then released into the atmosphere.
【００３３】＜工程３＞図４を参照して、前記原料混合
槽Ｂへの熱分解油の搬送の後、原料混合槽Ａにおいて、
混合物の溶融・反応が完了、つまり廃プラスチック原料
に含まれている特に塩化水素が全て離脱された後、該溶
融プラスチックは、熱分解槽４へ戻される。熱分解槽４
には、外部からの加熱手段により約４００〜４５０℃に
保たれ溶融プラスチックの熱分解反応が促進され、熱分
解ガスは、後流側に配設された接触分解槽４に搬送され
油化される。<Step 3> Referring to FIG. 4, after transporting the pyrolysis oil to the raw material mixing tank B, in the raw material mixing tank A,
After the melting / reaction of the mixture is completed, that is, after all the hydrogen chloride contained in the waste plastic raw material is removed, the molten plastic is returned to the thermal decomposition tank 4. Thermal decomposition tank 4
Is maintained at about 400 to 450 ° C. by a heating means from the outside to accelerate the thermal decomposition reaction of the molten plastic, and the thermal decomposition gas is conveyed to the catalytic decomposition tank 4 arranged on the downstream side and oilized. It
【００３４】＜工程４＞内部が空になった原料混合槽Ａ
には、前記＜工程１＞を繰り返し行う。<Step 4> Raw material mixing tank A having an empty inside
For this, <Step 1> is repeated.
【００３５】＜工程５＞前記原料混合槽Ａへの熱分解油
の搬送の後、原料混合槽Ｂにおいて、混合物の溶融・反
応が完了、つまり廃プラスチック原料に含まれている特
に塩化水素が全て離脱された後、該溶融プラスチック
は、熱分解槽４へ戻される。熱分解槽４には、外部から
の加熱手段により約４００〜４５０℃に保たれ溶融プラ
スチックの熱分解反応が促進され、熱分解ガスは、後流
側に配設された接触分解槽４に搬送され油化処理され
る。<Step 5> After the pyrolysis oil is conveyed to the raw material mixing tank A, in the raw material mixing tank B, the melting and reaction of the mixture are completed, that is, especially the hydrogen chloride contained in the waste plastic raw material is completely removed. After being detached, the molten plastic is returned to the thermal decomposition tank 4. In the thermal decomposition tank 4, the temperature is kept at about 400 to 450 ° C. by an external heating means to accelerate the thermal decomposition reaction of the molten plastic, and the thermal decomposition gas is conveyed to the catalytic decomposition tank 4 arranged on the downstream side. It is then oiled.
【００３６】＜工程６＞内部が空になった原料混合槽Ｂ
には、前記＜工程２＞を繰り返し行う。<Step 6> Raw material mixing tank B having an empty inside
For this, <Step 2> is repeated.
【００３７】上記の工程１から工程５を原料混合槽Ａ及
び原料混合槽Ｂでの繰り返しを行うことにより、熱分解
槽４において、連続的に安定した熱分解を行うことがで
き、その結果、連続的に安定した油化ができる。By repeating the above steps 1 to 5 in the raw material mixing tank A and the raw material mixing tank B, the thermal decomposition tank 4 can perform continuous and stable thermal decomposition. As a result, Oil can be continuously and stably converted.
【００３８】前記の各工程を図にしたものを図５に示
す。FIG. 5 shows a diagram of each of the above steps.
【００３９】なお、本実施例においては、原料混合槽の
数をＡ、Ｂの２つ配設し使用したが、連続した処理の途
中で、原料混合槽に投入する廃プラスチック原料に含ま
れている特に塩化水素等の量が異なる場合は、原料混合
槽をもう一つ余分に配設しておくと容易に連続処理に対
応することができる。In this embodiment, two raw material mixing tanks, A and B, were provided and used, but they are included in the waste plastic raw material to be put into the raw material mixing tank during the continuous treatment. Especially when the amounts of hydrogen chloride and the like are different, it is possible to easily cope with continuous processing by arranging another extra raw material mixing tank.
【００４０】この場合の各工程を図６に示す。Each step in this case is shown in FIG.
【００４１】溶融・混合槽での廃プラスチックの滞留時
間をより大きく取ることにより、高塩化水素混入プラス
チックでの高い脱塩化水素除去率を得ることができる。By taking a longer residence time of the waste plastic in the melting / mixing tank, it is possible to obtain a high dehydrochlorination removal rate in the plastic with a high hydrogen chloride content.
【００４２】[0042]
（１）原料混合槽において、廃プラスチック原料に含ま
れている特に塩化水素等を完全に除去することができ、
後流側に脱塩化水素等の除去の設備が不要となるととも
に、製品の油化中に脱塩化水素等が混入することがなく
なり、製品の品質が高品位で安定する。(1) In the raw material mixing tank, especially hydrogen chloride contained in the waste plastic raw material can be completely removed,
Equipment for removing dehydrochlorination etc. is not required on the downstream side, and dehydrochlorination etc. is not mixed in during oilification of the product, and the quality of the product is stable and high quality.
【００４３】（２）高価で保守が複雑な押出機を使用し
なくても、安価で保守の容易な原料混合槽を１つ増設す
ることにより連続処理が可能となる。(2) Even if an expensive and complicated maintenance is not required, continuous processing can be performed by adding one raw material mixing tank which is inexpensive and easy to maintain.
【図１】 本発明の廃プラスチックの油化処理設備の全
体概要図を示す。FIG. 1 shows an overall schematic diagram of a waste plastic oil treatment facility of the present invention.
【図２】 本発明の廃プラスチックの油化処理設備を使
用した油化処理方法の工程説明図を示す。FIG. 2 is a process explanatory view of an oil treatment method using the waste plastic oil treatment equipment of the present invention.
【図３】 本発明の廃プラスチックの油化処理設備を使
用した油化処理方法の工程説明図を示す。FIG. 3 is a process explanatory view of an oil treatment method using the waste plastic oil treatment equipment of the present invention.
【図４】 本発明の廃プラスチックの油化処理設備を使
用した油化処理方法の工程説明図を示す。FIG. 4 is a process explanatory view of an oil treatment method using the waste plastic oil treatment equipment of the present invention.
【図５】 原料混合槽Ａ、Ｂでの工程簡略図を示す。FIG. 5 shows a simplified process diagram in the raw material mixing tanks A and B.
【図６】 原料混合槽Ａ、Ｂ、Ｃでの工程簡略図を示
す。FIG. 6 shows a simplified process diagram in the raw material mixing tanks A, B, and C.
【図７】 従来の油化処理設備の全体概要図を示す。FIG. 7 shows an overall schematic view of a conventional oil treatment facility.
１ 押出機 ２ 原料混合槽 ３ 熱分解槽 ４ 接触分解槽 ５ ポンプ ６ バルブ ７ 排風機 ８ 水洗塔 ９ 原料投入口 １０ 回転式攪拌機 １１ 自己循環手段 1 Extruder 2 Raw Material Mixing Tank 3 Pyrolysis Tank 4 Catalytic Cracking Tank 5 Pump 6 Valve 7 Blower 8 Water Washing Tower 9 Raw Material Inlet 10 Rotating Stirrer 11 Self Circulating Means
───────────────────────────────────────────────────── 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 Ｃ０８Ｊ 11/12 ＺＡＢ 7310−4Ｆ (72)発明者 武内 隆春 福岡県北九州市戸畑区大字中原46−59 新 日本製鐵株式会社機械・プラント事業部内 (72)発明者 白水 渡 福岡県北九州市戸畑区大字中原46番地の59 日鐵プラント設計株式会社内─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification number Internal reference number FI Technical indication location C08J 11/12 ZAB 7310-4F (72) Inventor Takaharu Takeuchi 46, Nakahara, Tobata-ku, Kitakyushu, Fukuoka Prefecture 59 Nippon Steel Co., Ltd., Machinery & Plant Division (72) Inventor Wataru Shiramizu 59 Nippon Steel Plant Design Co., Ltd., 46 Nakahara, Tobata-ku, Kitakyushu, Fukuoka Prefecture
Claims (1)
少なくとも２個以上の原料混合槽を配設し、該原料混合
槽の後流側に熱分解槽及び接触分解槽を直列に連設し、
前記熱分解槽と前記複数の原料混合槽とを両者の内容物
を循環せしめるように接続し、前記原料混合槽に内容物
の攪拌手段およびまたは自己循環手段を設けるとともに
塩化水素の除去手段を配設してなる廃プラスチックの油
化製造設備。1. At least two raw material mixing tanks having a waste plastic charging port on the upper part thereof are arranged, and a thermal decomposition tank and a catalytic decomposition tank are connected in series on the downstream side of the raw material mixing tanks,
The thermal decomposition tank and the plurality of raw material mixing tanks are connected so as to circulate the contents of both, and the raw material mixing tank is provided with a stirring means and / or a self-circulating means for the contents and a hydrogen chloride removing means. Equipment for oil production of waste plastics.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24542593A JP2922760B2 (en) | 1993-09-30 | 1993-09-30 | Waste plastic oil production facility |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24542593A JP2922760B2 (en) | 1993-09-30 | 1993-09-30 | Waste plastic oil production facility |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH07102264A true JPH07102264A (en) | 1995-04-18 |
| JP2922760B2 JP2922760B2 (en) | 1999-07-26 |
Family
ID=17133470
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP24542593A Expired - Fee Related JP2922760B2 (en) | 1993-09-30 | 1993-09-30 | Waste plastic oil production facility |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2922760B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20030010364A (en) * | 2001-07-26 | 2003-02-05 | 김동춘 | Sulfuration apparatus by cracking reaction of atalyzer-down type and fabrication method for volatile-oil·whale-oil thereby |
| KR100517898B1 (en) * | 2001-07-31 | 2005-09-30 | 김범진 | Downflow type catalytic cracking reaction apparatus and method for producing gasoline and light oil using waste synthetic resins using the same |
| KR100782381B1 (en) * | 2006-08-03 | 2007-12-07 | 한국에너지기술연구원 | Method and apparatus for improving fuel quality of pyrolysis reclaimed fuel from wasted plastic and reclaimed fuel manufactured thereof |
| CN111750358A (en) * | 2020-05-29 | 2020-10-09 | 浙江科茂环境科技有限公司 | Waste plastic green oiling technology embedded garbage incineration method |
-
1993
- 1993-09-30 JP JP24542593A patent/JP2922760B2/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20030010364A (en) * | 2001-07-26 | 2003-02-05 | 김동춘 | Sulfuration apparatus by cracking reaction of atalyzer-down type and fabrication method for volatile-oil·whale-oil thereby |
| KR100517898B1 (en) * | 2001-07-31 | 2005-09-30 | 김범진 | Downflow type catalytic cracking reaction apparatus and method for producing gasoline and light oil using waste synthetic resins using the same |
| KR100782381B1 (en) * | 2006-08-03 | 2007-12-07 | 한국에너지기술연구원 | Method and apparatus for improving fuel quality of pyrolysis reclaimed fuel from wasted plastic and reclaimed fuel manufactured thereof |
| CN111750358A (en) * | 2020-05-29 | 2020-10-09 | 浙江科茂环境科技有限公司 | Waste plastic green oiling technology embedded garbage incineration method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2922760B2 (en) | 1999-07-26 |
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