JPH06220461A - Production of hydrocarbon oil from waste plastic or rubber material and equipment for use therein - Google Patents
Production of hydrocarbon oil from waste plastic or rubber material and equipment for use thereinInfo
- Publication number
- JPH06220461A JPH06220461A JP5009238A JP923893A JPH06220461A JP H06220461 A JPH06220461 A JP H06220461A JP 5009238 A JP5009238 A JP 5009238A JP 923893 A JP923893 A JP 923893A JP H06220461 A JPH06220461 A JP H06220461A
- Authority
- JP
- Japan
- Prior art keywords
- hydrocarbon oil
- catalytic cracking
- waste plastic
- tank
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
- C10G57/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with polymerisation
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、廃物化されたプラスチ
ック材もしくはゴム材を再利用して炭化水素油を得る方
法、及び、その実施に使用される装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for reusing a waste plastic material or rubber material to obtain a hydrocarbon oil, and an apparatus used for carrying out the method.
【０００２】[0002]
【従来の技術】現代の自動車においては、車体パネル，
各種の内装部品，タイヤ等々が、高分子化合物であるプ
ラスチック材あるいはゴム材によって形成されたものと
されており、プラスチック材あるいはゴム材の使用比率
が次第に高められてきている。それゆえ、例えば、１台
の自動車がその役割を終えて廃車処分されるだけでも、
相当量の廃物とされたプラスチック材あるいはゴム材、
即ち、廃プラスチック材あるいは廃ゴム材が生じること
になり、日々多数の自動車が廃車処分される現状におい
ては、それによって生じる廃プラスチック材あるいは廃
ゴム材の量は莫大なものとなる。2. Description of the Related Art In modern automobiles, body panels,
Various interior parts, tires, etc. are supposed to be formed of a plastic material or a rubber material which is a high molecular compound, and the use ratio of the plastic material or the rubber material is gradually increasing. So, for example, if one car ends its role and is simply scrapped,
A considerable amount of waste plastic or rubber material,
That is, waste plastic materials or waste rubber materials are generated, and in the current situation where a large number of automobiles are disposed of as waste vehicles every day, the amount of waste plastic materials or waste rubber materials generated thereby becomes enormous.
【０００３】このように、自動車に関連して生じる分だ
けであっても莫大な量となる廃プラスチック材あるいは
廃ゴム材については、自動車業界をはじめ各種の業界に
おいて、種々の有効な再利用が図られており、さらに、
その再利用を一層拡大するための努力が払われている。
このような状況のもとで、廃プラスチック材あるいは廃
ゴム材の再利用の一環として、例えば、特開昭 63-1781
95号公報にも示される如くに、廃プラスチック材から炭
化水素油を生成することが提案されており、生成された
炭化水素油は、燃料等として用いられる。As described above, the waste plastic material or the waste rubber material, which is an enormous amount even if it is generated in connection with the automobile, can be effectively reused in various industries including the automobile industry. Is planned, and further,
Efforts are being made to further expand its reuse.
Under such circumstances, as a part of the recycling of waste plastic materials or waste rubber materials, for example, JP-A-63-1781
As shown in Japanese Patent Laid-Open No. 95, it has been proposed to produce a hydrocarbon oil from a waste plastic material, and the produced hydrocarbon oil is used as a fuel or the like.
【０００４】廃プラスチック材から炭化水素油を生成す
るにあたっては、従来、廃プラスチック材を熱分解し、
それによって生成された熱分解ガスを、さらに、適切な
触媒を用いたもとで接触分解し、それによって生成され
た接触分解ガスを冷却して、比較的低い沸点を有する炭
化水素油を得るようになすことが知られている。例え
ば、前述の特開昭 63-178195号公報に示されている方法
の場合には、プラスチック材の熱分解が、３９０℃〜５
００℃の範囲内の温度のもとで溶融液相にて行われ、ま
た、熱分解ガスの接触分解が、２００℃〜３５０℃の範
囲内の温度のもとで触媒としてゼオライトが用いられて
行われ、その結果、炭素原子数を２２以下とする低沸点
炭化水素油が得られるものとされている。なお、このよ
うにして、熱分解，接触分解及び冷却という工程をもっ
て炭化水素油を得る方法は、廃プラスチック材に対して
のみならず、廃ゴム材に対しても適用される。In producing hydrocarbon oil from waste plastic materials, conventionally, waste plastic materials are pyrolyzed,
The pyrolysis gas produced thereby is further catalytically cracked under the use of a suitable catalyst, and the catalytic cracking gas produced thereby is cooled to obtain a hydrocarbon oil having a relatively low boiling point. It is known. For example, in the case of the method disclosed in the above-mentioned Japanese Patent Laid-Open No. 63-178195, the thermal decomposition of the plastic material is 390 ° C to 5 ° C.
It is carried out in the molten liquid phase under a temperature in the range of 00 ° C, and the catalytic decomposition of the pyrolysis gas is carried out by using zeolite as a catalyst under the temperature in the range of 200 ° C to 350 ° C. As a result, a low boiling point hydrocarbon oil having 22 or less carbon atoms is supposed to be obtained. The method of obtaining hydrocarbon oil by the steps of thermal decomposition, catalytic decomposition and cooling in this way is applied not only to waste plastic materials but also to waste rubber materials.
【０００５】[0005]
【発明が解決しようとする課題】上述の如くにして、廃
プラスチック材あるいは廃ゴム材から炭化水素油が生成
されるに際しては、廃プラスチック材あるいは廃ゴム材
が熱分解されて生成される熱分解ガスの接触分解に用い
られるゼオライト等の触媒は、熱劣化を回避すべく、そ
の温度が廃プラスチック材あるいは廃ゴム材の熱分解が
行われる温度より低い所定の温度以下に維持される。そ
れゆえ、廃プラスチック材あるいは廃ゴム材の熱分解に
より生成された熱分解ガスが、接触分解されるにあたっ
て触媒により冷却され、それにより熱分解ガス中に含ま
れる高沸点炭化水素成分（ワックス成分）が触媒に付着
して、触媒の機能低下がきたされることになる。As described above, when hydrocarbon oil is produced from the waste plastic material or the waste rubber material, the pyrolysis produced by thermally decomposing the waste plastic material or the waste rubber material. The temperature of the catalyst such as zeolite used for catalytic cracking of gas is maintained below a predetermined temperature, which is lower than the temperature at which thermal decomposition of waste plastic material or waste rubber material is performed, in order to avoid thermal degradation. Therefore, the pyrolysis gas generated by the pyrolysis of the waste plastic material or the waste rubber material is cooled by the catalyst during the catalytic cracking, whereby the high boiling point hydrocarbon component (wax component) contained in the pyrolysis gas. Will adhere to the catalyst, resulting in deterioration of the function of the catalyst.
【０００６】そこで、接触分解用の触媒の機能低下を抑
制するための方策として、廃プラスチック材あるいは廃
ゴム材の熱分解が行われる温度を一層高めて、熱分解ガ
ス中における高沸点炭化水素成分の含有比率を低下さ
せ、接触分解用の触媒における高沸点炭化水素成分の付
着量を低減させることが考えられる。しかしながら、こ
のような方策がとられる場合には、廃プラスチック材あ
るいは廃ゴム材の熱分解により生成された熱分解ガスが
接触分解されて得られる接触分解ガス中における、冷却
されても炭化水素油に転化されずにガス状態を維持する
低沸点炭化水素成分の含有量が増大し、その結果、炭化
水素油の回収率が低下してしまうという不都合が生じる
ことになる。Therefore, as a measure for suppressing the deterioration of the function of the catalyst for catalytic cracking, the temperature at which the waste plastic material or the waste rubber material is pyrolyzed is further increased so that the high boiling point hydrocarbon component in the pyrolysis gas is increased. It is conceivable to reduce the content ratio of and reduce the amount of high-boiling point hydrocarbon components attached to the catalyst for catalytic cracking. However, if such measures are taken, the hydrocarbon oil, even when cooled, in the catalytic cracking gas obtained by catalytically cracking the thermal cracking gas generated by the thermal decomposition of waste plastic material or waste rubber material The content of the low-boiling-point hydrocarbon component that is not converted into the gaseous state and maintains the gas state increases, and as a result, the recovery rate of the hydrocarbon oil decreases, which is a disadvantage.
【０００７】斯かる点に鑑み、本発明は、廃プラスチッ
ク材あるいは廃ゴム材を熱分解して得られる熱分解ガス
を、適切な触媒を用いたもとで接触分解し、それにより
得られる接触分解ガスを冷却して炭化水素油を得るにあ
たり、接触分解用の触媒の熱劣化及び高沸点炭化水素成
分の付着による機能低下を効果的に抑制でき、しかも、
炭化水素油の回収率の向上を図ることができることにな
る、廃プラスチック又はゴム材から炭化水素油を得る方
法及びその実施に使用される装置を提供することを目的
とする。In view of such a point, the present invention is to catalytically decompose a thermal decomposition gas obtained by thermally decomposing a waste plastic material or a waste rubber material using an appropriate catalyst, and obtain a catalytic decomposition gas obtained thereby. When the hydrocarbon oil is cooled to obtain a hydrocarbon oil, it is possible to effectively suppress the thermal deterioration of the catalyst for catalytic cracking and the functional deterioration due to the adhesion of the high boiling hydrocarbon component, and
It is an object of the present invention to provide a method for obtaining a hydrocarbon oil from waste plastic or a rubber material, and an apparatus used for carrying out the method, which can improve the recovery rate of the hydrocarbon oil.
【０００８】[0008]
【課題を解決するための手段】上述の目的を達成すべ
く、本発明に係る廃プラスチック又はゴム材から炭化水
素油を得る方法は、廃物化されたプラスチック材もしく
はゴム材を４５０℃を超える温度のもとで熱分解して熱
分解生成物を得、さらに、得られた熱分解生成物を固体
酸触媒を用いたもとで接触分解して接触分解生成物を
得、得られた接触分解生成物に冷却処理を施して炭化水
素油と分解ガス成分とを得た後、得られた分解ガス成分
を重合触媒を用いてオリゴマー化して炭化水素油を得る
ものとされる。In order to achieve the above-mentioned object, a method for obtaining a hydrocarbon oil from waste plastic or rubber material according to the present invention is a method for treating waste plastic material or rubber material at a temperature exceeding 450 ° C. Thermal decomposition product to obtain a thermal decomposition product, and then the obtained thermal decomposition product is catalytically decomposed under a solid acid catalyst to obtain a catalytic decomposition product. After cooling treatment to obtain a hydrocarbon oil and a cracked gas component, the obtained cracked gas component is oligomerized using a polymerization catalyst to obtain a hydrocarbon oil.
【０００９】そして、本発明に係る廃プラスチック又は
ゴム材から炭化水素油を得る方法の好ましい例にあって
は、接触分解生成物を得る処理が、１２０℃〜２５０℃
の範囲内の温度のもとで行われる。In a preferred example of the method for obtaining a hydrocarbon oil from waste plastic or rubber material according to the present invention, the treatment for obtaining a catalytic cracking product is 120 ° C to 250 ° C.
Performed at a temperature within the range of.
【００１０】また、本発明に係る炭化水素油生成装置
は、廃物化されたプラスチック材もしくはゴム材が４５
０℃を超える温度のもとで熱分解されて熱分解生成物が
得られる熱分解部と、熱分解部において得られる熱分解
生成物が固体酸触媒が用いられたもとで接触分解されて
接触分解生成物が得られる接触分解部と、接触分解部に
おいて得られる接触分解生成物に冷却処理が施されて炭
化水素油と分解ガス成分とが得られる冷却部とに加え
て、冷却部において得られる分解ガス成分が重合触媒が
用いられたもとでオリゴマー化されて炭化水素油が得ら
れるオリゴマー化部が設けられ、さらに、冷却部におい
て得られる炭化水素油及びオリゴマー化部において得ら
れる炭化水素油が回収される炭化水素油回収部が設けら
れて構成される。Further, in the hydrocarbon oil producing apparatus according to the present invention, the waste plastic material or rubber material is 45
Pyrolysis part that is pyrolyzed at a temperature over 0 ° C. to obtain a pyrolysis product, and the pyrolysis product obtained in the pyrolysis part is catalytically decomposed under the use of a solid acid catalyst to catalytically decompose it. In addition to the catalytic cracking section where the product is obtained and the cooling section where the catalytic cracking product obtained in the catalytic cracking section is subjected to cooling treatment to obtain hydrocarbon oil and cracked gas components, it is obtained in the cooling section The cracked gas component is oligomerized under the use of a polymerization catalyst to provide an oligomerization section where hydrocarbon oil is obtained. Furthermore, the hydrocarbon oil obtained in the cooling section and the hydrocarbon oil obtained in the oligomerization section are recovered. A hydrocarbon oil recovery unit is provided and configured.
【００１１】そして、本発明に係る炭化水素油生成装置
の好ましい例にあっては、接触分解部が、１２０℃〜２
５０℃の範囲内の温度のもとで接触分解生成物が得られ
るものとされる。In a preferred example of the hydrocarbon oil generator according to the present invention, the catalytic cracking section has a temperature of 120 ° C to 2 ° C.
It is assumed that catalytic cracking products are obtained under temperatures in the range of 50 ° C.
【００１２】[0012]
【作用】上述の如くの本発明に係る廃プラスチック又は
ゴム材から炭化水素油を得る方法及び炭化水素油生成装
置にあっては、廃物化されたプラスチック材もしくはゴ
ム材が４５０℃を超える比較的高い温度のもとで熱分解
されて、熱分解生成物が得られ、また、熱分解生成物が
固体酸触媒が用いられ、例えば、１２０℃〜２５０℃の
範囲内の温度とされる比較的低い温度のもとで接触分解
されて、接触分解生成物が得られるようにされることに
より、熱分解生成物が、高沸点炭化水素成分の含有比率
が低下せしめられたものとされ、それにより、比較的低
い温度のもとでの接触分解にあたっても、接触分解用の
固体酸触媒の高沸点炭化水素成分の付着による機能低下
が効果的に抑制され、また、接触分解用の固体酸触媒が
比較的低い温度に維持されて、その熱劣化が効果的に抑
制される。さらに、接触分解生成物に冷却処理が施され
て炭化水素油と共に得られる分解ガス成分が、重合触媒
が用いられたもとでオリゴマー化されて炭化水素油を生
成するものとされるので、接触分解生成物に冷却処理が
施されて得られる炭化水素油に加えて、分解ガス成分の
オリゴマー化による炭化水素油が得られることになっ
て、炭化水素油の回収率の向上が図られることになる。In the method for obtaining hydrocarbon oil from waste plastic or rubber material and the hydrocarbon oil producing apparatus according to the present invention as described above, the waste plastic material or rubber material relatively exceeds 450 ° C. Pyrolysis under high temperature yields a pyrolysis product, and the pyrolysis product uses a solid acid catalyst, for example at a temperature in the range of 120 ° C to 250 ° C. By catalytically cracking at a low temperature to obtain a catalytic cracking product, the thermal cracking product is said to have a reduced content ratio of the high-boiling hydrocarbon component, whereby Even in catalytic cracking under relatively low temperature, the functional deterioration of the solid acid catalyst for catalytic cracking due to the high boiling point hydrocarbon component is effectively suppressed, and the solid acid catalyst for catalytic cracking is To a relatively low temperature Is lifting, the heat deterioration can be effectively suppressed. Further, the cracking gas component obtained by cooling the catalytic cracking product together with the hydrocarbon oil is oligomerized under the use of the polymerization catalyst to generate the hydrocarbon oil. In addition to the hydrocarbon oil obtained by subjecting the product to the cooling treatment, the hydrocarbon oil can be obtained by the oligomerization of the cracked gas component, so that the recovery rate of the hydrocarbon oil can be improved.
【００１３】[0013]
【実施例】図１は、本発明に係る廃プラスチック又はゴ
ム材から炭化水素油を得る方法の一例の実施に使用され
る、本発明に係る炭化水素油生成装置の一例を概略的に
示す。EXAMPLE FIG. 1 schematically shows an example of a hydrocarbon oil producing apparatus according to the present invention, which is used for carrying out an example of a method for obtaining a hydrocarbon oil from waste plastic or rubber material according to the present invention.
【００１４】図１に示される炭化水素油生成装置の一例
においては、例えば、ポリプロピレン等を含む廃物化さ
れたプラスチック材又は廃物化されたゴム材とされる再
生素材１１が貯蔵されたホッパ１２が備えられており、
そのホッパ１２に関連して、ホッパ１２から供給される
再生素材１１を、回動するスクリュー１３によって粉砕
するとともに熱分解槽１５に移送するスクリューコンベ
ア１４が設けられている。In an example of the hydrocarbon oil production apparatus shown in FIG. 1, a hopper 12 storing a recycled material 11 such as a waste plastic material containing polypropylene or a waste rubber material is stored. Is equipped,
In relation to the hopper 12, there is provided a screw conveyor 14 that crushes the recycled material 11 supplied from the hopper 12 by the rotating screw 13 and transfers it to the thermal decomposition tank 15.
【００１５】熱分解槽１５は、スクリューコンベア１４
における搬出部が連結された導入口部１５Ａが設けられ
た槽本体１５Ｂと導入口部１５Ａから槽本体１５Ｂの内
部に供給された再生素材１１を熱分解すべく加熱する加
熱部１６とにより構成されている。加熱部１６は、槽本
体１５Ｂに配されて槽本体１５Ｂの内部の温度を検出す
る温度センサ１７からの検出出力に基づいて、槽本体１
５Ｂ内における熱分解温度が４５０℃を超える所定の温
度に維持されるように温度調整制御が行われるものとさ
れている。The thermal decomposition tank 15 includes a screw conveyor 14
In the tank main body 15B provided with an inlet port 15A to which the unloading part is connected, and a heating unit 16 for heating the recycled material 11 supplied from the inlet port 15A to the inside of the tank main body 15B to thermally decompose it. ing. The heating unit 16 is arranged in the tank body 15B, and based on the detection output from the temperature sensor 17 that detects the temperature inside the tank body 15B, the tank body 1
The temperature adjustment control is performed so that the thermal decomposition temperature in 5B is maintained at a predetermined temperature exceeding 450 ° C.
【００１６】熱分解槽１５における槽本体１５Ｂの上方
部分は、槽本体１５Ｂ内に得られる熱分解生成物である
熱分解ガスの接触分解が行われる接触分解槽１８のガス
導入口部１８Ａに連結されている。接触分解槽１８に
は、固体酸触媒として塩化アルミニウム（ＡｌＣｌ3 ・
６Ｈ2 Ｏ）１９が内蔵されており、熱分解槽１５におけ
る槽本体１５Ｂからガス導入口部１８Ａを通じて供給さ
れる熱分解ガスが、塩化アルミニウム１９に接触して接
触分解される。接触分解槽１８は、それに配されて内部
の温度を検出する温度センサ２０からの検出出力に基づ
いて温度調整制御がなされる図示が省略された加熱部に
より、その内部における接触分解温度が１２０℃〜２５
０℃の範囲内に維持されるように加熱される。The upper portion of the tank main body 15B in the thermal decomposition tank 15 is connected to the gas inlet port 18A of the catalytic decomposition tank 18 in which the thermal decomposition gas, which is the thermal decomposition product obtained in the tank main body 15B, is catalytically decomposed. Has been done. In the catalytic cracking tank 18, aluminum chloride (AlCl 3
6H 2 O) 19 is built in, and the thermal decomposition gas supplied from the tank main body 15B in the thermal decomposition tank 15 through the gas introduction port 18A comes into contact with the aluminum chloride 19 and is catalytically decomposed. The catalytic cracking tank 18 has a catalytic cracking temperature of 120 ° C. inside thereof by a heating unit (not shown) whose temperature is controlled and controlled based on a detection output from a temperature sensor 20 which is arranged in the catalytic cracking tank 18. ~ 25
It is heated so as to be maintained within the range of 0 ° C.
【００１７】接触分解槽１８におけるガス送出口部１８
Ｂには、導管２１の一端が接続されている。導管２１
は、流量調整弁２２が設けられたものとされており、ま
た、その他端が、接触分解槽１８において得られる接触
分解生成物である接触分解ガスの冷却が行われる冷却器
２３の入口部に接続されている。そして、冷却器２３の
出口部は、導管２４を介して中和槽２５に通じている。
中和槽２５は、中和液として２０％水酸化ナトリウム
（ＮａＯＨ）水溶液２６を内蔵しており、また、２０％
水酸化ナトリウム水溶液２６を攪拌する回転攪拌器２７
を備えたものとされている。冷却器２３の出口部から伸
びた導管２４は、その先端が中和槽２５内における２０
％水酸化ナトリウム水溶液２６中にまで達するものとさ
れている。Gas outlet port 18 in catalytic cracking tank 18
One end of the conduit 21 is connected to B. Conduit 21
Is provided with a flow rate adjusting valve 22, and the other end is at the inlet of a cooler 23 where the catalytic cracking gas which is the catalytic cracking product obtained in the catalytic cracking tank 18 is cooled. It is connected. The outlet of the cooler 23 communicates with the neutralization tank 25 via the conduit 24.
The neutralization tank 25 contains a 20% sodium hydroxide (NaOH) aqueous solution 26 as a neutralization liquid, and also contains 20%.
A rotary stirrer 27 for stirring the sodium hydroxide aqueous solution 26.
It is said to be equipped with. The conduit 24 extending from the outlet of the cooler 23 has a tip of 20 in the neutralization tank 25.
It is said that it reaches up to the 26% aqueous solution of sodium hydroxide.
【００１８】中和槽２５の内部における中間部分は、導
管２８を介して、炭化水素油回収槽２９に通じており、
また、中和槽２５の内部における上方部分は、導管３０
を介して、オリゴマー化槽３１に通じている。オリゴマ
ー化槽３１は、重合触媒として１００％燐酸（Ｈ3 ＰＯ
4 ）３２を内蔵しており、また、１００％燐酸３２を攪
拌する回転攪拌器３３を備えたものとされている。さら
に、オリゴマー化槽３１は、図示が省略された加熱部に
より、その内部温度が１３０℃程度となるように加熱さ
れる。オリゴマー化槽３１の内部における中間部分は、
導管３４を介して、炭化水素油回収槽２９に通じてお
り、また、オリゴマー化槽３１の内部における上方部分
は、導管３５を介して、ブロア３６に通じている。そし
て、ブロア３６は、導管３７を介してアキュムレータ３
８に通じ、さらに、アキュムレータ３８は、導管３９を
介して熱分解槽１５における加熱部１６に通じるものと
されている。An intermediate portion inside the neutralization tank 25 leads to a hydrocarbon oil recovery tank 29 via a conduit 28,
In addition, the upper portion inside the neutralization tank 25 is the conduit 30.
Through the oligomerization tank 31. The oligomerization tank 31 uses 100% phosphoric acid (H 3 PO) as a polymerization catalyst.
4 ) 32 is built in, and a rotary stirrer 33 for stirring 100% phosphoric acid 32 is provided. Further, the oligomerization tank 31 is heated by a heating unit (not shown) so that the internal temperature thereof becomes about 130 ° C. The intermediate portion inside the oligomerization tank 31 is
It communicates with the hydrocarbon oil recovery tank 29 via a conduit 34, and the upper portion inside the oligomerization tank 31 communicates with a blower 36 via a conduit 35. The blower 36 is connected to the accumulator 3 via the conduit 37.
In addition, the accumulator 38 communicates with the heating section 16 of the thermal decomposition tank 15 via a conduit 39.
【００１９】このように構成される本発明に係る炭化水
素油生成装置の一例を使用して、本発明に係る廃プラス
チック又はゴム材から炭化水素油を得る方法の一例を実
施するにあたっては、先ず、ホッパ１２に貯蔵された再
生素材１１を、スクリューコンベア１４によって、熱分
解槽１５における槽本体１５Ｂに設けられた導入口部１
５Ａから槽本体１５Ｂ内に供給する。そして、熱分解槽
１５における加熱部１６によって槽本体１５Ｂを加熱
し、槽本体１５Ｂ内において再生素材１１の熱分解が行
われる状態となす。このとき、加熱部１６に対する温度
センサ１７からの検出出力に基づく温度調整制御が行わ
れて、槽本体１５Ｂ内における熱分解温度が４５０℃を
超える所定の温度に維持される状態となす。それによ
り、槽本体１５Ｂの内部には、再生素材１１の熱分解に
よる熱分解生成物である熱分解ガスが得られる。In carrying out an example of a method for obtaining a hydrocarbon oil from waste plastic or rubber material according to the present invention by using the example of the hydrocarbon oil producing apparatus according to the present invention thus constructed, first, Introducing the recycled material 11 stored in the hopper 12 into the tank body 15B of the thermal decomposition tank 15 by the screw conveyor 14
Supply from 5A into the tank body 15B. Then, the tank main body 15B is heated by the heating unit 16 in the thermal decomposition tank 15, so that the recycled material 11 is thermally decomposed in the tank main body 15B. At this time, the temperature adjustment control based on the detection output from the temperature sensor 17 to the heating unit 16 is performed so that the thermal decomposition temperature in the tank body 15B is maintained at a predetermined temperature exceeding 450 ° C. As a result, a pyrolysis gas that is a pyrolysis product of the pyrolysis of the recycled material 11 is obtained inside the tank body 15B.
【００２０】槽本体１５Ｂの内部に得られた熱分解ガス
は、接触分解槽１８に設けられたガス導入口部１８Ａを
通じて接触分解槽１８の内部に導入され、接触分解槽１
８に内蔵された固体酸触媒としての塩化アルミニウム１
９に接触し、その結果、接触分解槽１８において、熱分
解槽１５からの熱分解ガスの接触分解が行われる。この
とき、接触分解槽１８に設けられた加熱部に対する温度
センサ２０からの検出出力に基づく温度調整制御が行わ
れて、接触分解槽１８内における接触分解温度が１２０
℃〜２５０℃の範囲内に維持される状態となす。それに
より、接触分解槽１８の内部には、熱分解槽１５からの
熱分解ガスの接触分解による接触分解生成物である接触
分解ガスが得られる。The pyrolysis gas obtained inside the tank main body 15B is introduced into the inside of the catalytic cracking tank 18 through the gas introduction port 18A provided in the catalytic cracking tank 18, and the catalytic cracking tank 1
Aluminum chloride as a solid acid catalyst built in 8.
As a result, the catalytic decomposition of the thermal decomposition gas from the thermal decomposition tank 15 is performed in the catalytic decomposition tank 18. At this time, the temperature adjustment control based on the detection output from the temperature sensor 20 for the heating unit provided in the catalytic cracking tank 18 is performed, and the catalytic cracking temperature in the catalytic cracking tank 18 is 120.
The state is maintained within the range of ℃ to 250 ℃. As a result, inside the catalytic cracking tank 18, a catalytic cracking gas which is a catalytic cracking product by catalytic cracking of the thermal cracking gas from the thermal cracking tank 15 is obtained.
【００２１】接触分解槽１８の内部に得られた接触分解
ガスは、流量調整弁２２が設けられた導管２１を通じて
冷却器２３に供給され、冷却器２３によって冷却され
る。それにより、冷却器２３において、接触分解ガスに
基づく低沸点炭化水素油と、例えば、炭素原子数を３〜
４とする重合化合物を主成分とする分解ガス成分とを得
る。そして、冷却器２３において得られた低沸点炭化水
素油及び分解ガス成分を、導管２４を通じて、中和槽２
５に内蔵された中和液である２０％水酸化ナトリウム水
溶液２６中に供給する。中和槽２５内においては、底部
側から上方に向けて順次重なる、２０％水酸化ナトリウ
ム水溶液２６の層，冷却器２３からの低沸点炭化水素油
５０の層、及び、冷却器２３からの分解ガス成分５１の
層が形成される。The catalytic cracking gas obtained inside the catalytic cracking tank 18 is supplied to a cooler 23 through a conduit 21 provided with a flow rate adjusting valve 22 and cooled by the cooler 23. Thereby, in the cooler 23, the low boiling point hydrocarbon oil based on the catalytic cracking gas and, for example, the carbon atom number of 3 to
A decomposed gas component containing the polymer compound of No. 4 as the main component is obtained. Then, the low boiling point hydrocarbon oil and the cracked gas components obtained in the cooler 23 are passed through the conduit 24 to the neutralization tank 2
It is supplied into a 20% aqueous sodium hydroxide solution 26, which is a neutralizing solution contained in the No. 5 solution. In the neutralization tank 25, a layer of 20% aqueous sodium hydroxide solution 26, a layer of low-boiling hydrocarbon oil 50 from the cooler 23, and a decomposition from the cooler 23, which are sequentially stacked from the bottom side upward. A layer of gas component 51 is formed.
【００２２】このようにして中和槽２５内において中間
層を成して得られる低沸点炭化水素油５０を、導管２８
を通じて炭化水素油回収槽２９に供給するとともに、中
和槽２５内において最上層を成して得られる分解ガス成
分５１を、導管３０を通じて、オリゴマー化槽３１に内
蔵された重合触媒である１００％燐酸３２中に供給す
る。それにより、オリゴマー化槽３１内において、重合
触媒である１００％燐酸３２中での分解ガス成分５１の
オリゴマー化が行われて、分解ガス成分５１に基づく低
沸点炭化水素油が生成される。但し、中和槽２５からの
分解ガス成分５１の全てがオリゴマー化されるわけでは
なく、その一部は未反応分解ガス成分として残留する。
そのため、オリゴマー化槽３１内においては、底部側か
ら上方に向けて順次重なる、１００％燐酸３２の層，分
解ガス成分５１のオリゴマー化により生成された低沸点
炭化水素油５２の層、及び、未反応分解ガス成分５３の
層が形成される。The low boiling point hydrocarbon oil 50 obtained by forming the intermediate layer in the neutralization tank 25 in this manner is supplied to the conduit 28.
Is supplied to the hydrocarbon oil recovery tank 29 through the above, and the cracked gas component 51 obtained by forming the uppermost layer in the neutralization tank 25 is supplied through the conduit 30 to the polymerization catalyst 100% which is contained in the oligomerization tank 31. Supply in phosphoric acid 32. As a result, the cracked gas component 51 is oligomerized in the polymerization catalyst 100% phosphoric acid 32 in the oligomerization tank 31, and a low boiling point hydrocarbon oil based on the cracked gas component 51 is produced. However, not all of the decomposition gas component 51 from the neutralization tank 25 is oligomerized, and a part thereof remains as an unreacted decomposition gas component.
Therefore, in the oligomerization tank 31, a layer of 100% phosphoric acid 32, a layer of low-boiling hydrocarbon oil 52 produced by the oligomerization of the cracked gas component 51, and a layer of 100% phosphoric acid 32, which sequentially overlap from the bottom side upward, A layer of reactive decomposition gas component 53 is formed.
【００２３】このようにして、オリゴマー化槽３１内に
おいて中間層を成して得られる低沸点炭化水素油５２
を、導管３４を通じて炭化水素油回収槽２９に供給し、
炭化水素油回収槽２９内に、中和槽２５から導管２８を
通じて供給される低沸点炭化水素油５０とオリゴマー化
槽３１から導管３４を通じて供給される低沸点炭化水素
油５２とが、低沸点炭化水素油５５として回収される状
態となす。In this way, the low boiling point hydrocarbon oil 52 obtained by forming the intermediate layer in the oligomerization tank 31.
Is supplied to the hydrocarbon oil recovery tank 29 through a conduit 34,
In the hydrocarbon oil recovery tank 29, a low boiling point hydrocarbon oil 50 supplied from the neutralization tank 25 through the conduit 28 and a low boiling point hydrocarbon oil 52 supplied from the oligomerization tank 31 through the conduit 34 The hydrogen oil 55 is recovered.
【００２４】また、オリゴマー化槽３１内において最上
層を成して得られる未反応分解ガス成分５３を導管３５
を通じてブロワ３６に供給する。ブロワ３６に供給され
た未反応分解ガス成分５３は、ブロワ３６により導管３
７を通じてアキュムレータ３８に送り込まれ、さらに、
アキュムレータ３８から導管３９を介して熱分解槽１５
における加熱部１６に供給されて、加熱部１６において
再利用される。The unreacted decomposed gas component 53 obtained by forming the uppermost layer in the oligomerization tank 31 is introduced into the conduit 35.
Through the blower 36. The unreacted decomposed gas component 53 supplied to the blower 36 is supplied to the conduit 3 by the blower 36.
It is sent to the accumulator 38 through 7, and further
Pyrolysis tank 15 from accumulator 38 via conduit 39
Is supplied to the heating section 16 and is reused in the heating section 16.
【００２５】このようにして再生素材１１から生成さ
れ、炭化水素油回収槽２９に回収された低沸点炭化水素
油５５は、導管５６を通じて炭化水素油回収槽２９から
導出され、例えば、燃料として用いられる。The low boiling point hydrocarbon oil 55 thus produced from the recycled material 11 and recovered in the hydrocarbon oil recovery tank 29 is led out from the hydrocarbon oil recovery tank 29 through the conduit 56 and is used as a fuel, for example. To be
【００２６】上述の如くにして実施される本発明に係る
廃プラスチック又はゴム材から炭化水素油を得る方法に
おいて、再生素材１１の熱分解に際しての熱分解温度が
４５０℃を超える所定の温度とされ、また、再生素材１
１の熱分解により得られた熱分解ガスの接触分解に際し
ての接触分解温度が１２０℃〜２５０℃の範囲内とされ
るのは、先ず、再生素材１１の熱分解に際しての熱分解
温度が４５０℃以下である場合には、再生素材１１の熱
分解により得られる熱分解ガスが、高沸点炭化水素成分
の含有比率が高いものとなり、その接触分解にあたっ
て、高沸点炭化水素成分が接触分解用の固体酸触媒であ
る塩化アルミニウムに付着してその触媒機能を低下させ
る現象が顕著であることが実験により確認されたからで
あり、また、再生素材１１の熱分解により得られた熱分
解ガスの接触分解に際しての接触分解温度が１２０℃未
満である場合は、接触分解用の固体酸触媒として塩化ア
ルミニウムの活性化が充分に図られず、一方、再生素材
１１の熱分解により得られた熱分解ガスの接触分解に際
しての接触分解温度が２５０℃を超える場合には、接触
分解用の固体酸触媒として塩化アルミニウムの劣化が著
しくなることが実験的に確認されたからである。In the method for obtaining hydrocarbon oil from waste plastic or rubber material according to the present invention, which is carried out as described above, the thermal decomposition temperature at the thermal decomposition of the recycled material 11 is set to a predetermined temperature exceeding 450 ° C. , Again, recycled material 1
First, the catalytic decomposition temperature in the catalytic decomposition of the thermal decomposition gas obtained by the thermal decomposition of No. 1 is set in the range of 120 ° C. to 250 ° C. First, the thermal decomposition temperature in the thermal decomposition of the recycled material 11 is 450 ° C. In the following cases, the pyrolysis gas obtained by the pyrolysis of the recycled material 11 has a high content ratio of the high-boiling hydrocarbon component, and the high-boiling hydrocarbon component is solid for catalytic cracking during the catalytic cracking. This is because it was confirmed by experiments that the phenomenon of adhering to aluminum chloride, which is an acid catalyst, and reducing its catalytic function is remarkable, and also in the catalytic decomposition of the thermal decomposition gas obtained by the thermal decomposition of the recycled material 11. When the catalytic decomposition temperature of is less than 120 ° C, aluminum chloride cannot be sufficiently activated as a solid acid catalyst for catalytic decomposition, while the thermal decomposition of the recycled material 11 causes Was when the catalytic cracking temperature during catalytic cracking of the pyrolysis gas is higher than 250 ° C. This is because the deterioration of the aluminum chloride is remarkably as the solid acid catalyst for catalytic cracking was confirmed experimentally.
【００２７】次に、本願の発明者により行われた、本発
明に係る方法の一例に従って廃物化されたプラスチック
材から炭化水素油が生成される場合における炭化水素油
の回収率と、本発明に係る方法とは異なる方法に従って
廃物化されたプラスチック材から炭化水素油が生成され
る場合における炭化水素油の回収率と、の比較実験につ
いて述べる。Next, the recovery rate of the hydrocarbon oil when the hydrocarbon oil is produced from the plastic material scrapped according to an example of the method according to the present invention, which was carried out by the inventor of the present application, and the present invention A comparison experiment of the hydrocarbon oil recovery rate in the case where hydrocarbon oil is produced from a plastic material that has been scrapped according to a method different from the above method will be described.
【００２８】斯かる比較実験は、図２に示される実験装
置が用いられて行われた。図２に示される実験装置にあ
っては、環状炉６０及び６１が備えられ、環状炉６０及
び６１の夫々の内部には、両者に亙る管状部材６２が配
されており、その管状部材６２の両端部には、栓部材６
３及び６４を介して導管６５の一端部側及び導管６６の
一端部側が夫々連結されている。そして、導管６６の他
端部側は、栓部材６７により開口部が閉塞された容器６
８内に、栓部材６７を貫通して配されている。容器６８
の開口部を閉塞する栓部材６７には、それを貫通する一
端部側を有した他の導管６９も係合しており、この導管
６９の他端部側は、栓部材７０を介してフラスコ７１の
内部に挿入されている。Such a comparative experiment was carried out by using the experimental apparatus shown in FIG. In the experimental apparatus shown in FIG. 2, annular furnaces 60 and 61 are provided, and tubular members 62 are disposed inside the annular furnaces 60 and 61, respectively. Plug members 6 are provided at both ends.
One end side of the conduit 65 and one end side of the conduit 66 are connected via 3 and 64, respectively. The other end of the conduit 66 has a container 6 whose opening is closed by a plug member 67.
8 is disposed so as to penetrate the stopper member 67. Container 68
The plug member 67 for closing the opening of the is also engaged with another conduit 69 having one end side penetrating therethrough, and the other end side of this conduit 69 is connected via a stopper member 70 to the flask. It is inserted inside 71.
【００２９】フラスコ７１は、磁気攪拌装置７２上に載
置された油槽７３内に置かれており、油槽７３内にはヒ
ータ７４も配されている。そして、フラスコ７１の内部
には、磁気攪拌装置７２によって遠隔駆動される攪拌子
７５が配されており、また、フラスコ７１の内部には、
一端部側が開放された導管７６の他端部側も栓部材７７
を貫通して挿入されている。The flask 71 is placed in an oil tank 73 placed on a magnetic stirrer 72, and a heater 74 is also arranged in the oil tank 73. A stirrer 75, which is remotely driven by the magnetic stirrer 72, is arranged inside the flask 71, and inside the flask 71,
The other end of the conduit 76 whose one end is open is also connected to the plug member 77.
Has been inserted through.
【００３０】そして、斯かる実験装置が用いられての第
１の実験状態においては、本発明に係る方法の一例に従
って廃物化されたプラスチック材から炭化水素油を生成
すべく、管状部材６２の内部における、環状炉６０の内
部に対向する位置に、廃物化されたプラスチック材であ
るポリプロピレン８０の５０ｇが配されるとともに、環
状炉６１の内部に対向する位置に、固体酸触媒として塩
化アルミニウム８１が所定量をもって配された。また、
容器６８内には、中和液として２０％水酸化ナトリウム
水溶液８２が所定量をもって入れられるとともに、フラ
スコ７１内には、重合触媒として１００％燐酸８３が所
定量をもって入れられた。そして、油槽７３内に配され
たヒータ７４が、フラスコ７１の内部を略１３０℃に維
持すべく加熱状態をとるものとされ、また、磁気攪拌装
置７２がフラスコ７１の内部における１００％燐酸８３
中の攪拌子７５を遠隔駆動する状態とされ、さらに、導
管６５を通じて窒素（Ｎ2 ）ガスが管状部材６２内に吹
き込まれるもとで、環状炉６０の炉内温度が５００℃に
設定されるとともに環状炉６１の炉内温度が２５０℃に
設定された。Then, in the first experimental state in which such an experimental apparatus is used, the inside of the tubular member 62 is produced in order to produce hydrocarbon oil from the waste plastic material according to an example of the method according to the present invention. In the above, 50 g of polypropylene 80, which is a waste plastic material, is disposed at a position facing the inside of the ring furnace 60, and aluminum chloride 81 as a solid acid catalyst is placed at a position facing the inside of the ring furnace 61. Arranged in a predetermined amount. Also,
A predetermined amount of 20% sodium hydroxide aqueous solution 82 was put in the container 68 as a neutralizing solution, and a predetermined amount of 100% phosphoric acid 83 was put in the flask 71 as a polymerization catalyst. Then, the heater 74 arranged in the oil tank 73 is brought into a heated state so as to maintain the inside of the flask 71 at approximately 130 ° C., and the magnetic stirring device 72 causes the 100% phosphoric acid 83 in the inside of the flask 71.
The stirrer 75 therein is driven remotely, and further, while the nitrogen (N 2 ) gas is blown into the tubular member 62 through the conduit 65, the furnace temperature of the annular furnace 60 is set to 500 ° C. At the same time, the temperature inside the annular furnace 61 was set to 250 ° C.
【００３１】その結果、容器６８内及びフラスコ７１内
の夫々に低沸点炭化水素油が得られ、また、フラスコ７
１に設けられた導管７６を通じて未反応分解ガスが回収
された。そして、容器６８内及びフラスコ７１内の夫々
に得られた低沸点炭化水素油を回収して重量を計測した
ところ、略４３．５ｇであった。従って、ポリプロピレ
ン８０の５０ｇに対する回収された低沸点炭化水素油の
重量の割合（回収率）は、略４３．５ｇ×１００／５０
ｇ ＝ 略８７％であった。As a result, low boiling point hydrocarbon oil is obtained in the container 68 and the flask 71, respectively.
Unreacted decomposed gas was recovered through the conduit 76 provided in No. 1. Then, the low boiling point hydrocarbon oil obtained in each of the container 68 and the flask 71 was collected and weighed, and it was about 43.5 g. Therefore, the ratio of the weight of the recovered low boiling point hydrocarbon oil to 50 g of polypropylene 80 (recovery rate) is about 43.5 g × 100/50.
g = about 87%.
【００３２】また、上述の実験装置が用いられての第２
の実験状態においては、本発明に係る方法とは異なる方
法に従って廃物化されたプラスチック材から炭化水素油
を生成すべく、管状部材６２の内部における、環状炉６
０の内部に対応する位置に、廃物化されたプラスチック
材であるポリプロピレン８０の５０ｇが配されるととも
に、環状炉６１の内部に対向する位置に、固体酸触媒と
して塩化アルミニウム８１が所定量をもって配され、容
器６８内には中和液として２０％水酸化ナトリウム水溶
液８２が所定量をもって入れられたが、フラスコ７１，
油槽７３及び磁気攪拌装置７２は撤去された。そして、
導管６５を通じて窒素ガスが管状部材６２内に吹き込ま
れるもとで、環状炉６０の炉内温度が５００℃に設定さ
れるとともに環状炉６１の炉内温度が２５０℃に設定さ
れた。In addition, a second device using the above-mentioned experimental device is used.
In the experimental state of 1., in order to produce hydrocarbon oil from waste plastic material according to a method different from the method according to the present invention, the annular furnace 6 is formed inside the tubular member 62.
50 g of polypropylene 80, which is a waste plastic material, is arranged at a position corresponding to the inside of 0, and aluminum chloride 81 as a solid acid catalyst is arranged at a predetermined amount at a position facing the inside of the annular furnace 61. Then, a predetermined amount of 20% aqueous sodium hydroxide solution 82 was put in the container 68 as a neutralizing solution.
The oil tank 73 and the magnetic stirring device 72 have been removed. And
While the nitrogen gas was blown into the tubular member 62 through the conduit 65, the temperature inside the annular furnace 60 was set to 500 ° C. and the temperature inside the annular furnace 61 was set to 250 ° C.
【００３３】その結果、容器６８内に低沸点炭化水素油
が得られ、また、容器６８内に設けられた導管６９を通
じて未反応分解ガスが回収された。そして、容器６８内
に得られた低沸点炭化水素油を回収して重量を計測した
ところ、略３０．０ｇであった。従って、ポリプロピレ
ン８０の５０ｇに対する回収された低沸点炭化水素油の
重量の割合（回収率）は、略３０．０ｇ×１００／５０
ｇ ＝ 略６０％であった。As a result, low boiling point hydrocarbon oil was obtained in the container 68, and unreacted cracked gas was recovered through the conduit 69 provided in the container 68. Then, the low boiling point hydrocarbon oil obtained in the container 68 was recovered and weighed, and it was about 30.0 g. Therefore, the ratio of the weight of the recovered low boiling point hydrocarbon oil to 50 g of polypropylene 80 (recovery rate) is about 30.0 g × 100/50.
g = about 60%.
【００３４】斯かる比較実験結果により、本発明に係る
方法の一例に従って廃物化されたプラスチック材から炭
化水素油が生成される場合における炭化水素油の回収率
が、本発明に係る方法とは異なる方法に従って廃物化さ
れたプラスチック材から炭化水素油が生成される場合に
おける炭化水素油の回収率に比して著しく向上されたも
のとされることが確認された。From the results of such comparative experiments, the recovery rate of the hydrocarbon oil when the hydrocarbon oil is produced from the waste plastic material according to the example of the method of the present invention is different from that of the method of the present invention. It was confirmed that the recovery rate was significantly improved as compared with the recovery rate of the hydrocarbon oil when the hydrocarbon oil was produced from the waste plastic material according to the method.
【００３５】[0035]
【発明の効果】以上の説明から明らかな如くに、本発明
に係る廃プラスチック又はゴム材から炭化水素油を得る
方法、及び、本発明に係る炭化水素油生成装置にあって
は、廃物化されたプラスチック材もしくはゴム材が、４
５０℃を超える比較的高い温度のもとで熱分解され、そ
れにより得られる熱分解生成物が、例えば、１２０℃〜
２５０℃の範囲内の温度とされる比較的低い温度のもと
で固体酸触媒が用いられて接触分解されるので、熱分解
生成物が、高沸点炭化水素成分の含有比率が低下せしめ
られたものとされ、それにより、比較的低い温度のもと
での接触分解にあたっても、接触分解用の固体酸触媒の
高沸点炭化水素成分の付着による機能低下が効果的に抑
制されるとともに、接触分解用の固体酸触媒が比較的低
い温度に維持されて、その熱劣化が効果的に抑制され
る。さらに、熱分解生成物が固体酸触媒が用いられたも
とで接触分解されて得られる接触分解生成物に冷却処理
が施されることにより、炭化水素油と分解ガス成分とが
得られるが、得られた分解ガス成分が、重合触媒が用い
られたもとでオリゴマー化されて炭化水素油を生成する
ものとされるので、接触分解生成物に冷却処理が施され
て得られる炭化水素油に加えて、分解ガス成分のオリゴ
マー化による炭化水素油が得られることになって、炭化
水素油の回収率の著しい向上が図られることになる。As is apparent from the above description, the method for obtaining hydrocarbon oil from waste plastic or rubber material according to the present invention and the hydrocarbon oil producing apparatus according to the present invention are made into waste. 4 plastic or rubber materials
The thermal decomposition product obtained by thermal decomposition under a relatively high temperature of more than 50 ° C. is, for example, 120 ° C.
Since the solid acid catalyst is catalytically cracked at a relatively low temperature within the range of 250 ° C., the thermal decomposition product is reduced in the content ratio of the high boiling hydrocarbon component. As a result, even in catalytic cracking at relatively low temperatures, functional degradation due to the adhesion of high boiling hydrocarbon components of the solid acid catalyst for catalytic cracking is effectively suppressed, and catalytic cracking is also performed. The solid acid catalyst for use is maintained at a relatively low temperature, and its thermal deterioration is effectively suppressed. Further, the thermal cracking product is catalytically cracked under the use of a solid acid catalyst, and the catalytic cracking product obtained is subjected to a cooling treatment to obtain a hydrocarbon oil and a cracked gas component. The cracked gas component is said to be oligomerized under the use of a polymerization catalyst to produce a hydrocarbon oil.In addition to the hydrocarbon oil obtained by cooling the catalytic cracking product, The hydrocarbon oil can be obtained by the oligomerization of the gas component, and the recovery rate of the hydrocarbon oil can be significantly improved.
【図１】本発明に係る廃プラスチック又はゴム材から炭
化水素油を得る方法の一例の実施に使用される、本発明
に係る炭化水素油生成装置の一例を示す概略構成図であ
る。FIG. 1 is a schematic configuration diagram showing an example of a hydrocarbon oil production apparatus according to the present invention used for carrying out an example of a method for obtaining a hydrocarbon oil from waste plastic or rubber material according to the present invention.
【図２】本発明に係る廃プラスチック又はゴム材から炭
化水素油を得る方法と他の廃プラスチックから炭化水素
油を得る方法との比較に用いられた実験装置を示す構成
図である。FIG. 2 is a configuration diagram showing an experimental apparatus used for comparison between a method for obtaining a hydrocarbon oil from waste plastic or a rubber material according to the present invention and a method for obtaining a hydrocarbon oil from another waste plastic.
１１ 再生素材 １２ ホッパ １４ スクリューコンベア １５ 熱分解槽 １５Ｂ 槽本体 １６ 加熱部 １８ 接触分解槽 １９ 塩化アルミニウム ２３ 冷却器 ２５ 中和槽 ２６ ２０％水酸化ナトリウム水溶液 ２９ 炭化水素油回収槽 ３１ オリゴマー化槽 ３２ １００％燐酸 ５０，５２，５５ 低沸点炭化水素油 11 Recycled Material 12 Hopper 14 Screw Conveyor 15 Thermal Decomposition Tank 15B Tank Main Body 16 Heating Section 18 Contact Decomposition Tank 19 Aluminum Chloride 23 Cooler 25 Neutralization Tank 26 20% Sodium Hydroxide Aqueous Solution 29 Hydrocarbon Oil Recovery Tank 31 Oligomerization Tank 32 100% phosphoric acid 50,52,55 low boiling point hydrocarbon oil
───────────────────────────────────────────────────── フロントページの続き (72)発明者 福島 立人 広島県安芸郡府中町新地３番１号 マツダ 株式会社内 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Tatsuto Fukushima 3-1, Shinchi, Fuchu-cho, Aki-gun, Hiroshima Prefecture Mazda Motor Corporation
Claims (4)
材を４５０℃を超える温度のもとで熱分解して熱分解生
成物を得、さらに、該熱分解生成物を固体酸触媒を用い
て接触分解して接触分解生成物を得、該接触分解生成物
に冷却処理を施して炭化水素油と分解ガス成分とを得た
後、上記分解ガス成分を重合触媒を用いてオリゴマー化
して炭化水素油を得ることを特徴とする廃プラスチック
又はゴム材から炭化水素油を得る方法。1. A waste plastic material or rubber material is thermally decomposed at a temperature exceeding 450 ° C. to obtain a thermal decomposition product, and the thermal decomposition product is contacted with a solid acid catalyst. After cracking to obtain a catalytic cracking product, the catalytic cracking product is subjected to a cooling treatment to obtain a hydrocarbon oil and a cracked gas component, and then the cracked gas component is oligomerized using a polymerization catalyst to give a hydrocarbon oil. A method for obtaining a hydrocarbon oil from waste plastic or rubber material, which comprises:
２５０℃の範囲内の温度のもとで行うことを特徴とする
請求項１記載の廃プラスチック又はゴム材から炭化水素
油を得る方法。2. The treatment for obtaining a catalytic decomposition product is carried out at 120 ° C.
The method for obtaining a hydrocarbon oil from waste plastic or rubber material according to claim 1, wherein the method is carried out at a temperature in the range of 250 ° C.
材が４５０℃を超える温度のもとで熱分解され、熱分解
生成物が得られる熱分解部と、 該熱分解部において得られる熱分解生成物が固体酸触媒
が用いられたもとで接触分解され、接触分解生成物が得
られる接触分解部と、 該接触分解部において得られる接触分解生成物に冷却処
理が施され、炭化水素油と分解ガス成分とが得られる冷
却部と、 該冷却部において得られる分解ガス成分が重合触媒が用
いられたもとでオリゴマー化され、炭化水素油が得られ
るオリゴマー化部と、 上記冷却部において得られる炭化水素油及び上記オリゴ
マー化部において得られる炭化水素油が回収される炭化
水素油回収部と、を備えて構成される炭化水素油生成装
置。3. A thermal decomposition part in which a waste plastic material or rubber material is thermally decomposed at a temperature exceeding 450 ° C. to obtain a thermal decomposition product, and a thermal decomposition product obtained in the thermal decomposition part. The substance is catalytically cracked under the use of a solid acid catalyst to obtain a catalytic cracking product, and the catalytic cracking product obtained in the catalytic cracking unit is subjected to a cooling treatment to give hydrocarbon oil and cracked gas. And a hydrocarbon part obtained in the cooling part, and a cooling part in which the components are obtained, an cracked gas component obtained in the cooling part is oligomerized under the use of a polymerization catalyst to obtain a hydrocarbon oil, and a hydrocarbon oil obtained in the cooling part. And a hydrocarbon oil recovery section for recovering the hydrocarbon oil obtained in the oligomerization section.
内の温度のもとで接触分解生成物が得られるものとされ
ることを特徴とする請求項３記載の炭化水素油生成装
置。4. The hydrocarbon oil production apparatus according to claim 3, wherein the catalytic cracking section is adapted to obtain a catalytic cracking product at a temperature in the range of 120 ° C. to 250 ° C. .
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5009238A JPH06220461A (en) | 1993-01-22 | 1993-01-22 | Production of hydrocarbon oil from waste plastic or rubber material and equipment for use therein |
| EP94100382A EP0607862A1 (en) | 1993-01-22 | 1994-01-12 | Method of obtaining hydrocarbon oil from waste plastic material or waste rubber material and apparatus used for carrying out the method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5009238A JPH06220461A (en) | 1993-01-22 | 1993-01-22 | Production of hydrocarbon oil from waste plastic or rubber material and equipment for use therein |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH06220461A true JPH06220461A (en) | 1994-08-09 |
Family
ID=11714827
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5009238A Pending JPH06220461A (en) | 1993-01-22 | 1993-01-22 | Production of hydrocarbon oil from waste plastic or rubber material and equipment for use therein |
Country Status (2)
| Country | Link |
|---|---|
| EP (1) | EP0607862A1 (en) |
| JP (1) | JPH06220461A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20010087776A (en) * | 2001-04-18 | 2001-09-26 | 김전열 | distillation- emulsifying technology through catalyst |
| CN104371750A (en) * | 2013-08-12 | 2015-02-25 | 上海金匙环保科技股份有限公司 | Pyrolysis reaction device, system and method thereof |
| CN108239552A (en) * | 2018-02-11 | 2018-07-03 | 宁波普前环保科技有限公司 | A kind of method for the treatment of of waste plastics and cellulose |
| CN108251146A (en) * | 2018-02-11 | 2018-07-06 | 宁波普前环保科技有限公司 | A kind of method of waste plastics and cellulose coprocessing |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1999009116A1 (en) * | 1997-08-13 | 1999-02-25 | Li Xing | Process and apparatus for producing hydrocarbon oil from organic or high molecular waste material |
| RU2202589C2 (en) * | 1998-09-24 | 2003-04-20 | ЖОУ Дингли | Method and device for production of hydrocarbons from domestic garbage or wastes and/or wastes of organic materials |
| IT1312096B1 (en) * | 1999-04-23 | 2002-04-04 | Tianfu Jiang | PROCEDURE AND PLANTS FOR THE CONVERSION OF WASTES INTO PLASTIC MATERIAL, INTO FUEL HYDROCARBONS. |
| CN1074447C (en) * | 1999-06-08 | 2001-11-07 | 周鼎力 | Process and equipment for producing gasoline and diesel oil with waste plastics and/or heavy oil |
| CN2408118Y (en) * | 1999-07-16 | 2000-11-29 | 周继福 | Equipment for producing gasoline and diesel oil by using waste plaste and/or heavy oil |
| JP2001220102A (en) | 2000-02-02 | 2001-08-14 | Matsumura Shuzo | Method and device for producing synthetic gas |
| CN1487988A (en) * | 2001-01-22 | 2004-04-07 | 姜天夫 | Method and apparatus for converting plastic garbage into hydrocarbon oil |
| CN1397627A (en) * | 2001-07-23 | 2003-02-19 | 北京国硕科技开发有限责任公司 | Process and equipment for preparing gasoline and diesel oil from waste plastics and/or heavy oil |
| FR2845391B1 (en) * | 2002-10-07 | 2006-05-12 | Inst Francais Du Petrole | PROCESS AND PLANT FOR PRODUCING SYNTHESIS GAS DEPOLLUED FROM A CHARGE RICH IN ORGANIC MATERIAL |
| CN101812314B (en) * | 2009-02-20 | 2013-06-19 | 上海金匙环保科技股份有限公司 | Low-temperature catalytic cracking method with high-value utilization of waste tire |
| KR20120080158A (en) * | 2009-06-19 | 2012-07-16 | 이노베이티브 에너지 솔루션즈 인코포레이티드 | Thermo-catalytic cracking for conversion of higher hydrocarbons into lower hydrocarbons |
| CN102205341A (en) * | 2011-01-30 | 2011-10-05 | 福州索源智能装备技术开发有限公司 | Intelligentized solid organic waste microwave cracking system and its production technology |
| CN116348573A (en) | 2020-09-28 | 2023-06-27 | 切弗朗菲利浦化学公司 | Use of recycled chemicals or polymers from pyrolysis plastic waste and mass balance accounting to allow the resulting product to be counted as recycled |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2357630A1 (en) * | 1976-07-05 | 1978-02-03 | Erap | Catalytic cracking in presence of rubber pyrolysis oil - from waste tyre material, giving improved yield of gasoline |
| US4851601A (en) * | 1988-01-19 | 1989-07-25 | Mobil Oil Corporation | Processing for producing hydrocarbon oils from plastic waste |
| GB8908081D0 (en) * | 1989-04-11 | 1989-05-24 | Shell Int Research | Process for the conversion of a hydrocarbonaceous feedstock |
-
1993
- 1993-01-22 JP JP5009238A patent/JPH06220461A/en active Pending
-
1994
- 1994-01-12 EP EP94100382A patent/EP0607862A1/en not_active Withdrawn
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20010087776A (en) * | 2001-04-18 | 2001-09-26 | 김전열 | distillation- emulsifying technology through catalyst |
| CN104371750A (en) * | 2013-08-12 | 2015-02-25 | 上海金匙环保科技股份有限公司 | Pyrolysis reaction device, system and method thereof |
| CN104371750B (en) * | 2013-08-12 | 2017-03-08 | 上海金匙环保科技股份有限公司 | Pyrolytic reaction device and its System and method for |
| CN108239552A (en) * | 2018-02-11 | 2018-07-03 | 宁波普前环保科技有限公司 | A kind of method for the treatment of of waste plastics and cellulose |
| CN108251146A (en) * | 2018-02-11 | 2018-07-06 | 宁波普前环保科技有限公司 | A kind of method of waste plastics and cellulose coprocessing |
| CN108239552B (en) * | 2018-02-11 | 2019-09-17 | 北京石油化工学院 | A kind of method for the treatment of of waste plastics and cellulose |
| CN108251146B (en) * | 2018-02-11 | 2019-09-17 | 北京石油化工学院 | A kind of method of waste plastics and cellulose coprocessing |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0607862A1 (en) | 1994-07-27 |
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