JPH09286991A - Production of fuel using waste plastic and apparatus therefor - Google Patents
Production of fuel using waste plastic and apparatus thereforInfo
- Publication number
- JPH09286991A JPH09286991A JP34862896A JP34862896A JPH09286991A JP H09286991 A JPH09286991 A JP H09286991A JP 34862896 A JP34862896 A JP 34862896A JP 34862896 A JP34862896 A JP 34862896A JP H09286991 A JPH09286991 A JP H09286991A
- Authority
- JP
- Japan
- Prior art keywords
- raw material
- oil
- volatile oil
- diesel oil
- waste 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.)
- Pending
Links
- 239000004033 plastic Substances 0.000 title claims abstract description 42
- 229920003023 plastic Polymers 0.000 title claims abstract description 42
- 239000002699 waste material Substances 0.000 title claims abstract description 35
- 239000000446 fuel Substances 0.000 title claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 20
- 239000000341 volatile oil Substances 0.000 claims abstract description 59
- 239000002283 diesel fuel Substances 0.000 claims abstract description 56
- 239000002994 raw material Substances 0.000 claims abstract description 49
- 238000005336 cracking Methods 0.000 claims abstract description 44
- 238000000034 method Methods 0.000 claims abstract description 27
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 19
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 18
- 238000010438 heat treatment Methods 0.000 claims abstract description 16
- 239000003921 oil Substances 0.000 claims abstract description 16
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 15
- 238000009835 boiling Methods 0.000 claims abstract description 15
- 238000007670 refining Methods 0.000 claims description 24
- 239000003054 catalyst Substances 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 13
- 238000004821 distillation Methods 0.000 claims description 11
- -1 polyethylene Polymers 0.000 claims description 8
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 5
- 238000000354 decomposition reaction Methods 0.000 claims description 5
- 229910018072 Al 2 O 3 Inorganic materials 0.000 claims description 4
- 239000004698 Polyethylene Substances 0.000 claims description 4
- 229910004283 SiO 4 Inorganic materials 0.000 claims description 4
- 229920000573 polyethylene Polymers 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 4
- 239000004743 Polypropylene Substances 0.000 claims description 3
- 239000004793 Polystyrene Substances 0.000 claims description 3
- 229920001155 polypropylene Polymers 0.000 claims description 3
- 229920002223 polystyrene Polymers 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 2
- 238000010298 pulverizing process Methods 0.000 claims 2
- 238000004523 catalytic cracking Methods 0.000 abstract description 4
- 238000003912 environmental pollution Methods 0.000 abstract description 4
- 238000000746 purification Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 11
- 239000000498 cooling water Substances 0.000 description 7
- 239000007788 liquid Substances 0.000 description 6
- 239000006229 carbon black Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 235000019645 odor Nutrition 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000004484 Briquette Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229920006328 Styrofoam Polymers 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000012634 fragment Substances 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000010705 motor oil Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000002085 persistent effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 239000002985 plastic film Substances 0.000 description 1
- 229920006255 plastic film Polymers 0.000 description 1
- 239000013502 plastic waste Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000008261 styrofoam Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 239000003440 toxic substance Substances 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
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Processing Of Solid Wastes (AREA)
- Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は廃プラスチックを用
いて燃料を製造する方法及び装置に係り、特に廃プラス
チックを原料として接触分解プロセス（catalytic crac
king process) によって揮発油やディーゼル油などの低
沸点炭化水素油を製造する方法及び装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for producing fuel using waste plastic, and more particularly to a catalytic cracking process using waste plastic as a raw material.
king process) to produce a low boiling point hydrocarbon oil such as volatile oil or diesel oil.
【０００２】[0002]
【従来の技術】石油化学工業の発達に伴って人類の日常
生活に欠かせない必須品のプラスチック製品は、沢山の
長所にも拘わらず焼却時有毒物質の発生、自然状態にお
ける難分解性のためにその廃棄物の処理が大きい社会問
題として台頭してきた。従って、廃プラスチックの再生
乃至再活性問題は単純なエネルギー節約の次元を越えて
プラスチック廃棄物処理の一番理想的な方策として最近
先進各国の主要関心事になっている。2. Description of the Related Art With the development of the petrochemical industry, essential plastic products, which are indispensable for humans' daily life, have many advantages, because of the generation of toxic substances during incineration and their persistent decomposition in nature. The disposal of the waste has emerged as a major social problem. Therefore, the problem of recycling or reactivating waste plastic has become a major concern of developed countries recently as the most ideal strategy for plastic waste treatment beyond the simple energy saving dimension.
【０００３】廃プラスチックの再活用方法には、廃プラ
スチックの粉末を溶融させた後射出機を通してプラスチ
ック製品に再生する方法があるが、このように単なる物
理的変換のみによる再生ではその利用性に限界がある。
一方、一定の条件でプラスチックの構成成分である高分
子炭化水素を分解及び変形させて低分子の有用な揮発油
やディーゼル油などを生産することのできる化学的方法
があるが、最近その実用化が活発に推進されている。後
者の代表的な例としては、韓国特許公告９６−３６０５
号，米国特許第５，４１４，１６９号，米国特許第５，
２８６，３７４号などに開示された方法または装置を挙
げることができる。これらの内容をまとめてみると、細
かく粉砕した可塑性プラスチック或いはゴム廃棄物を触
媒の存在下に高温で分解、蒸留して低沸騰点炭化水素油
やカーボンブラック(carbon black)、液化ガスなどを回
収することができるということである。但し、触媒の種
類とその処理時期及び方法、クラッキング時の温度及び
圧力、スラッジ（sludge)乃至ろう質物（waxy subspanc
e) の生成抑制方法などはそれぞれの発明によって差が
あり、石油化学工業の性格上これらの微細な差異は最終
分解蒸留産物の成分別回収率及びその品質に強く影響を
及ぼす。従って、この分野の発明で考慮すべき主眼点
は、前記の微細な差異を如何に調節して、経済的で安全
な方法で高品質の目的とする分解蒸留産物を多量回収し
得るかである。As a method of reusing waste plastics, there is a method of melting powders of waste plastics and then recycling them into plastic products through an injection machine. However, such recycling by only physical conversion limits the usability. There is.
On the other hand, there is a chemical method that can produce useful low molecular weight volatile oil or diesel oil by decomposing and deforming high molecular hydrocarbon which is a constituent of plastic under certain conditions. Is actively promoted. A typical example of the latter is Korean Patent Publication 96-3605.
U.S. Pat. No. 5,414,169, U.S. Pat. No. 5,
The method or apparatus disclosed in, for example, No. 286,374 can be mentioned. Summarizing these contents, finely crushed plastic or rubber waste is decomposed at high temperature in the presence of a catalyst and distilled to recover low boiling point hydrocarbon oil, carbon black, liquefied gas, etc. It means that you can do it. However, the type of catalyst and its treatment time and method, temperature and pressure during cracking, sludge or waxy subspanc
The methods for suppressing the formation of e) differ depending on the invention, and due to the nature of the petrochemical industry, these minute differences strongly affect the recovery rate and quality of each component of the final cracked distillation product. Therefore, the main point to be considered in the invention of this field is how to adjust the above-mentioned minute differences so as to recover a large amount of the target decomposition and distillation product of high quality in an economical and safe manner. .
【０００４】本発明者はこのような側面に着目して、第
１に使用操作が簡単で安全であり、第２に運転費用が低
廉であり、第３に高品質の揮発油とディーゼル油が多量
回収できる廃プラスチックを用いた燃料製造方法及び装
置の開発を目標として研究に着手し、本発明を完成し
た。韓国特許公告９６−１３６０５号に開示されている
ように、クラッキングプロダクトの生産速度を高めるた
めにクラッキングファーネス（cracking furnace)の温
度を４００℃以上上げると、ワックス（wax)のような重
質物質の生成が増加して、クラッキングファーネスの外
へ排出された時に凝縮器や配管などを封鎖するおそれが
ある。このため、できる限りクラッキングファーネス内
でより低沸点の成分に充分分解されるようにする必要が
ある。The present inventor pays attention to such aspects, firstly, the operation is simple and safe, secondly, the operating cost is low, and thirdly, high-quality volatile oil and diesel oil are used. The present invention has been completed by carrying out research aiming at the development of a fuel manufacturing method and apparatus using waste plastic that can be collected in large quantities. As disclosed in Korean Patent Publication No. 96-13605, when the temperature of a cracking furnace is increased by 400 ° C. or more to increase the production rate of cracking products, heavy substances such as wax may be generated. There is a risk that the production will increase and block condensers and piping when discharged out of the cracking furnace. Therefore, it is necessary to sufficiently decompose the components having a lower boiling point in the cracking furnace as much as possible.
【０００５】[0005]
【発明が解決しようとする課題】従って、本発明はかか
る諸欠点を克服するためのもので、その目的はＳｉＯ2
＋Ａｌ2Ｏ3 ＋Ａｌ2 （ＳｉＯ4 ) 3 からなる触媒を廃
プラスチックの粉末または断片に接触させてクラッキン
グリアクション（cracking reaction)を向上させること
によりワックス（wax)などの重質物質の生成を大幅に減
少させるとともに、安全確保のためにクラッキングファ
ーネスの周囲に防爆幕或いは爆破防止幕を設置して安全
確保、環境汚染の防止、及びエネルギーの効率的な再活
性を図ることのできる、廃プラスチックを用いた燃料製
造方法を提供することにある。SUMMARY OF THE INVENTION Therefore, the present invention is intended to overcome such drawbacks, and its purpose is SiO 2
The catalyst consisting of + Al 2 O 3 + Al 2 (SiO 4 ) 3 is brought into contact with powder or fragments of waste plastic to improve the cracking reaction, thereby significantly producing heavy substances such as wax. Along with reducing the number of waste plastics, a explosion-proof screen or explosion-proof screen is installed around the cracking furnace to ensure safety, prevent environmental pollution, and reactivate energy efficiently. The present invention is to provide a fuel manufacturing method.
【０００６】本発明の他の目的は、前記廃プラスチック
を用いた燃料製造方法を具現することのできる、廃プラ
スチックを用いた燃料製造装置を提供することにある。Another object of the present invention is to provide a fuel manufacturing apparatus using waste plastic, which can embody the fuel manufacturing method using the waste plastic.
【０００７】[0007]
【課題を解決するための手段】このような本発明の目的
は、供給原料を洗浄及び粉砕する工程と、前記洗浄及び
粉砕工程で設けられた原料をクラッキングファーネスに
原料を供給する工程と、触媒の存在下に原料を加熱して
分解蒸留過程を経て低沸点炭化水素油にクラッキング
（cracking) させる分解蒸留工程と、分解蒸留した低沸
点炭化水素油を揮発油とディーゼル油に分離する精留工
程と、前記精留された高温の揮発油とディーゼル油を冷
却する冷却工程と、冷却された揮発油とディーゼル油を
精製する精製工程とを含んでなることを特徴とする廃プ
ラスチックを用いた燃料製造方法によって達成される。An object of the present invention is to wash and grind a feed material, to feed the raw material provided in the washing and grinding step to a cracking furnace, and to provide a catalyst. In the presence of methane, a raw material is heated in the presence of a cracking distillation process to crack the low boiling point hydrocarbon oil through a cracking distillation process, and a rectification process that separates the cracked and distilled low boiling point hydrocarbon oil into volatile oil and diesel oil. And a cooling step of cooling the rectified high-temperature volatile oil and diesel oil, and a refining step of refining the cooled volatile oil and diesel oil, a fuel using waste plastic. This is achieved by the manufacturing method.
【０００８】本発明の他の目的は、原料供給装置と、前
記原料供給装置に連結された螺旋形原料供給器と、前記
螺旋形原料供給器から供給される原料をクラッキング
（cracking) させるクラッキングファーネスと、前記ク
ラッキングファーネスを加熱する加熱炉と、前記クラッ
キングファーネスから生成された低沸点炭化水素油を精
留する精留塔と、前記精留塔で精留された高温の揮発油
を冷却する揮発油冷却器と、前記精留塔で精留された高
温のディーゼル油を冷却するディーゼル油冷却器と、
前記揮発油冷却器で冷却された揮発油を精製する揮発油
精製装置と、前記ディーゼル油冷却器で冷却されたディ
ーゼル油を精製するディーゼル油精製装置とを含む廃プ
ラスチックを用いた燃料製造装置によって達成される。Another object of the present invention is to provide a raw material supply device, a spiral raw material supply device connected to the raw material supply device, and a cracking furnace for cracking the raw material supplied from the spiral raw material supply device. A heating furnace for heating the cracking furnace, a rectification column for rectifying the low boiling point hydrocarbon oil produced from the cracking furnace, and a volatilization for cooling the high temperature volatile oil rectified in the rectification column. An oil cooler, a diesel oil cooler for cooling the high temperature diesel oil rectified in the rectification tower,
A fuel production apparatus using waste plastic, comprising a volatile oil refining device for refining volatile oil cooled by the volatile oil cooler and a diesel oil refining device for refining diesel oil cooled by the diesel oil cooler To be achieved.
【０００９】[0009]
【発明の実施の形態】以下、添付図面を参照して本発明
を詳細に説明する。本発明で原料として使用する廃プラ
スチックはポリエチレン、ポリプロピレン、及びポリス
チレンなどを材料とした全ての廃棄プラスチック製品で
あって、農業用プラスチックフィルム、プラスチックバ
ック（plastic bags) 、家庭用プラスチック食器類、パ
ッケージ用スチロフォーム（styrofoam)などをその例と
して挙げることができる。但し、不燃焼性プラスチック
製品は除かれる。DETAILED DESCRIPTION OF THE INVENTION The present invention will be described in detail below with reference to the accompanying drawings. The waste plastics used as a raw material in the present invention are all waste plastic products made of polyethylene, polypropylene, polystyrene, etc., such as agricultural plastic films, plastic bags, household plastic tableware, and packaging. Styrofoam can be mentioned as an example. However, non-combustible plastic products are excluded.
【００１０】図１は本発明の好ましい実施例による燃料
製造装置の全体概略図である。図１によれば、本発明の
燃料製造装置は、廃プラスチック原料が投入される原料
供給装置１０と、前記原料供給装置１０の原料を移送さ
せる螺旋形原料供給器２０と、加熱炉４０及びその上部
のクラッキングファーネス（cracking furnace) ３０
と、前記クラッキングファーネス３０から生成された低
沸点炭化水素が注入される精留塔５０と、前記精留塔５
０の上部と下部に連設されており、前記精留塔５０で精
留された高温の揮発油及びディーゼル油を冷却する揮発
油冷却器６０及びディーゼル油冷却器７０と、前記それ
ぞれの冷却器６０，７０に連結されており、前記揮発油
冷却器６０とディーゼル冷却器７０を経て冷却された揮
発油及びディーゼル油をそれぞれ精製する揮発油精製装
置８０とディーゼル油精製装置９０とから構成される。FIG. 1 is an overall schematic view of a fuel production apparatus according to a preferred embodiment of the present invention. According to FIG. 1, the fuel production apparatus of the present invention comprises a raw material supply device 10 into which a waste plastic raw material is charged, a spiral raw material supply device 20 for transferring the raw material of the raw material supply device 10, a heating furnace 40 and its heating furnace 40. Upper cracking furnace 30
A rectification column 50 into which the low boiling point hydrocarbons generated from the cracking furnace 30 are injected, and the rectification column 5
0 connected to the upper part and the lower part of 0, a volatile oil cooler 60 and a diesel oil cooler 70 for cooling the high temperature volatile oil and diesel oil rectified in the rectification tower 50, and the respective coolers. It is connected to 60 and 70, and comprises a volatile oil refining device 80 and a diesel oil refining device 90 for refining the volatile oil and diesel oil cooled through the volatile oil cooler 60 and the diesel cooler 70, respectively. .
【００１１】前記螺旋形原料供給器２０は通常のプロペ
ラ式供給器であり、駆動モータ２１によって原料を移送
して、クラッキングファーネス３０に投入される原料の
注入量を適切に調節する。前記クラッキングファーネス
３０は分子篩隔板と材料散布管から構成されており、安
全確保のために防爆幕を設置することができる。また、
前記クラッキングファーネス３０の下には加熱炉４０が
設けられ、練炭ボイラまたは他のボイラによって熱量の
供給を受けることが出来るようになっている。前記クラ
ッキングファーネス３０でどろりとした液体になる原料
は精留塔５０を経るが、この精留塔５０は揮発油及びデ
ィーゼル油混合体を液体に漉した後、揮発油やディーゼ
ル油の示範精留過程を根拠として揮発油、ディーゼル
油、そして液化ガスを分離する。この分離された液化ガ
スは精留塔５０の最上端から排出され、揮発油は精留塔
５０の上部に連結された揮発油冷却器６０へ供給される
一方、ディーゼル油は精留塔５０の下部に連結されたデ
ィーゼル油冷却器７０へ供給される。The spiral raw material feeder 20 is a general propeller type feeder, and the raw material is transferred by a drive motor 21 to appropriately adjust the amount of raw material injected into the cracking furnace 30. The cracking furnace 30 is composed of a molecular sieve partition plate and a material spray tube, and an explosion-proof screen can be installed to ensure safety. Also,
A heating furnace 40 is provided below the cracking furnace 30 so that a heating amount can be supplied by a briquette boiler or another boiler. The raw material which becomes a thick liquid in the cracking furnace 30 passes through a rectification tower 50. The rectification tower 50 strains a mixture of volatile oil and diesel oil into a liquid, and then rectifies volatile oil or diesel oil. Separation of volatile oil, diesel oil, and liquefied gas based on the process. The separated liquefied gas is discharged from the uppermost end of the rectification tower 50, the volatile oil is supplied to the volatile oil cooler 60 connected to the upper portion of the rectification tower 50, while the diesel oil is discharged from the rectification tower 50. It is supplied to the diesel oil cooler 70 connected to the lower part.
【００１２】揮発油冷却器６０とディーゼル油冷却器７
０は、高温の揮発油とディーゼル油が流動するその冷却
管６１，７１の外部へ冷却水を供給して冷却する。即
ち、図面に示すように、揮発油冷却器６０とディーゼル
油冷却器７０はそのケース６２，７２の下部に冷却水供
給弁６３，７３が連結されており、冷却水を供給して高
温の揮発油及びディーゼル油を冷却する。この揮発油及
び冷却水を冷却し、熱くなった冷却水は冷却器ケース６
２，７２の上部に配設された冷却水排出管６４，７４を
通じて外部へ排出される。Volatile oil cooler 60 and diesel oil cooler 7
0 supplies cooling water to the outside of the cooling pipes 61 and 71 through which high-temperature volatile oil and diesel oil flow and cools. That is, as shown in the drawings, the volatile oil cooler 60 and the diesel oil chiller 70 have cooling water supply valves 63 and 73 connected to the lower portions of their cases 62 and 72, respectively, to supply cooling water and evaporate at high temperature. Cool oil and diesel oil. The volatile oil and cooling water are cooled, and the hot cooling water is cooled by the cooler case 6
The water is discharged to the outside through the cooling water discharge pipes 64 and 74 arranged on the upper portions of the 2, 72.
【００１３】前記精留塔５０、揮発油精製装置８０、及
びディーゼル油精製装置９０は通常の石油精製施設と同
様の原理で構成される。前記原料供給装置１０と螺旋形
原料供給器２０は原料供給システムを構成し、クラッキ
ングファーネス３０と加熱炉４０はクラッキングシステ
ムを構成し、精留塔５０及びその付帯設備は分溜系統を
構成し、揮発油冷却器６０及びディーゼル油冷却器７０
は冷却系統を、そして揮発油精製装置８０及びディーゼ
ル油精製装置９０は精製系統を構成する。The rectification tower 50, the volatile oil refining device 80, and the diesel oil refining device 90 are constructed on the same principle as that of an ordinary petroleum refining facility. The raw material supply device 10 and the spiral raw material supply device 20 constitute a raw material supply system, the cracking furnace 30 and the heating furnace 40 constitute a cracking system, and the rectification column 50 and its auxiliary equipment constitute a fractionation system. Volatile oil cooler 60 and diesel oil cooler 70
Constitutes a cooling system, and the volatile oil refining device 80 and the diesel oil refining device 90 constitute a refining system.
【００１４】このように構成された本発明の燃料製造装
置を用いて燃料を製造する本方法は次の５工程からな
る。第１工程は洗浄及び粉砕工程である。この工程は供
給される原料の供給に適した状態に作る工程であり、ゴ
ミ場などから収集した廃プラスチックを切断機、洗浄
機、及び圧縮乾燥機などの浄化装置を通して綺麗に洗浄
乾燥し、切断機や粉砕機を用いて細かく切る。勿論、綺
麗なプラスチックの場合には水で洗う必要はない。The present method for producing fuel using the fuel production apparatus of the present invention thus constructed comprises the following five steps. The first step is a washing and crushing step. This process is a process that makes it suitable for supplying the raw materials to be supplied, and cleans and dries the waste plastic collected from the garbage place through a purifying device such as a cutting machine, a washing machine, and a compression dryer, and then cuts it. Use a machine or a crusher to cut into small pieces. Of course, clean plastic does not need to be washed with water.
【００１５】第２工程は原料供給工程であり、洗浄及び
粉砕工程で準備された原料をクラッキングファーネス３
０まで供給する工程である。詳しくは、粉砕された廃プ
ラスチックは原料供給装置１０に一次供給され、次に螺
旋形原料供給器２０を通じてクラッキングファーネス３
０へ廃プラスチックが適切に分配注入される。第３工程
は分解蒸留工程であり、原料を加熱して分解蒸留過程を
経て低沸点炭化水素分子に分解蒸留する工程である。つ
まり、クラッキング工程であって、一般に熱分解（ther
mal cracking) 、水素化分解（hydro cracking) 、及び
接触分解（catalytic cracking) などの方法を採用する
が、本発明では熱と触媒を用いたクラッキング方法を使
用した。粉砕した原料をクラッキングファーネス３０に
入れると、加熱炉４０から供給される熱によって原料が
溶けてどろりとした液体になる。この時、本発明で使用
する触媒は熱分解反応速度を加速化する役割を果たす。
加熱された溶融プラスチックは３５０〜４５０℃の高熱
による分解蒸留過程を経て高分子アルカン（alkane) 類
が低分子炭化水素に分解蒸留される。The second step is a raw material supplying step, in which the raw material prepared in the cleaning and crushing step is used for the cracking furnace 3
This is a process of supplying 0. In detail, the crushed waste plastic is primarily supplied to the raw material supply device 10, and then is fed through the spiral raw material supply device 20 to the cracking furnace 3.
The waste plastic is properly distributed and injected into 0. The third step is a cracking distillation step, which is a step of heating the raw material and subjecting it to a cracking distillation process to cracking distillation to low-boiling point hydrocarbon molecules. In other words, it is a cracking process, and in general, pyrolysis (ther
Although methods such as mal cracking), hydrocracking, and catalytic cracking are adopted, in the present invention, a cracking method using heat and a catalyst is used. When the crushed raw material is put into the cracking furnace 30, the raw material is melted by the heat supplied from the heating furnace 40 and becomes a thick liquid. At this time, the catalyst used in the present invention serves to accelerate the thermal decomposition reaction rate.
The heated molten plastics are decomposed and distilled by high heat of 350 to 450 ° C. to decompose high molecular weight alkanes into low molecular weight hydrocarbons.
【００１６】ＳｉＯ2 ＋Ａｌ2Ｏ3 ＋Ａｌ2 （Ｓｉ
Ｏ4 ）3 を主要構成成分とする触媒は、クラッキング速
度を増加させるだけでなく、分解生成物における低沸点
炭化水素芳香属化合物及び分枝型炭化水素の含量を増加
させ、そして、ワックス成分を減少させることにより、
高オクタン価の良質の揮発油を多量生産し得るようにす
る作用をする。また、脱水素作用によって約１０〜１５
％のカーボンブラック（carbon black)も副産物として
得ることができる。SiO 2 + Al 2 O 3 + Al 2 (Si
O 4 ) 3 -based catalysts not only increase the cracking rate, but also increase the content of low boiling hydrocarbon aromatic compounds and branched hydrocarbons in the decomposition products, and increase the wax content. By reducing
It works to enable mass production of high-quality high-octane volatile oil. Also, about 10 to 15 due to dehydrogenation
% Carbon black can also be obtained as a by-product.
【００１７】第４工程は分離工程であり、分解蒸留した
低沸点炭化水素を精留塔５０に注入して揮発油及びディ
ーゼル油の混合体の液体に漉した後、揮発油とディーゼ
ル油の典型的な精留工程にかけて揮発油、ディーゼル
油、及び液化ガスを分離し、精留塔５０の頂上から出た
液化ガスは約１０〜１５％、精留塔５０の上部から出た
揮発油は約３０〜４５％、及び精留塔５０の下部から出
たディーゼル油は約３０〜４５％を占有する。１トンの
綺麗な廃プラスチックは３２０〜３７５kgを生産する。
産油率は７０〜８０％になり、液化ガスは水封じ（wate
r-sealing)または完全燃焼させるか或いは専用施設を増
設して液体に圧縮して、ＬＰＧ筒に入れて販売すること
もできる。The fourth step is a separation step, in which low-boiling point hydrocarbons that have been cracked and distilled are injected into the rectification column 50 and filtered into a liquid of a mixture of volatile oil and diesel oil. Volatile oil, diesel oil, and liquefied gas are separated through a conventional rectification step, and the liquefied gas from the top of the rectification tower 50 is about 10 to 15%, and the volatile oil from the top of the rectification tower 50 is about 30-45% and diesel oil exiting the bottom of the rectification column 50 occupy about 30-45%. One ton of clean waste plastic produces 320-375 kg.
The oil production rate is 70-80%, and the liquefied gas is sealed with water (wate
R-sealing) or complete combustion, or a dedicated facility can be added to compress into liquid and put in an LPG cylinder for sale.
【００１８】第５工程は冷却及び精製工程であり、精留
塔５０から分離した高温の揮発油とディーゼル油を、そ
れぞれ揮発油冷却器６０及びディーゼル油冷却器７０を
経て揮発油精製装置８０とディーゼル油精製装置９０へ
供給し、そこから精製して匂い及び色素を除去すること
により、自動車に使える揮発油や高品質のディーゼル油
などに商品化する工程である。The fifth step is a cooling and refining step, in which the high-temperature volatile oil and diesel oil separated from the rectification column 50 are passed through a volatile oil cooler 60 and a diesel oil cooler 70, respectively, to a volatile oil refining device 80. This is a process of supplying to a diesel oil refining device 90, refining it to remove odors and pigments, and commercializing it into volatile oil that can be used in automobiles and high-quality diesel oil.
【００１９】勿論、前記の各工程は通常の自動化装置を
用いて自動化することができる。Of course, each of the above steps can be automated by using a normal automation device.
【００２０】[0020]
【実施例】実施例１ 図１に示したような装置を用いて実験した。洗浄乾燥し
たポリエチレン（polyethylene) 廃プラスチック製品を
切断機と粉砕機を用いて細かく粉砕した後、２０kgの廃
プラスチック切片を原料供給装置１０と螺旋形原料供給
器２０を通じて、クラッキングファーネス３０へ連続的
に供給した。クラッキングファーネスはその下部に設置
された加熱炉から供給された熱で約４００℃を保持する
ようにした。溶融された廃プラスチック切片は３５０〜
４００℃の温度で低沸点炭化水素油に分解蒸留された。
この時、ＳｉＯ2 ＋Ａｌ2Ｏ3 ＋Ａｌ2 （ＳｉＯ4 ）3
を成分とする触媒を投入した。触媒投入の結果、分解蒸
留速度が増加し、分解蒸留された炭化水素油内のワック
ス成分が減少しただけでなく、揮発油のオクタン価が高
くなり、脱水素作用の結果、2.５kgのカーボンブラック
が生成された。EXAMPLES Example 1 An experiment was carried out using an apparatus as shown in FIG. The washed and dried polyethylene waste plastic product was finely crushed using a cutter and a crusher, and 20 kg of waste plastic pieces were continuously fed to the cracking furnace 30 through the raw material supply device 10 and the spiral raw material supply device 20. Supplied. The cracking furnace was kept at about 400 ° C. by the heat supplied from the heating furnace installed under the cracking furnace. Molten waste plastic pieces are 350 ~
It was cracked and distilled into a low boiling hydrocarbon oil at a temperature of 400 ° C.
At this time, SiO 2 + Al 2 O 3 + Al 2 (SiO 4 ) 3
A catalyst containing as a component was added. As a result of introducing the catalyst, not only the cracking distillation rate increased, the wax component in the hydrocarbon oil cracked and distilled decreased, but the octane number of the volatile oil also increased, and as a result of dehydrogenation, 2.5 kg of carbon black Was generated.
【００２１】分解蒸留された炭化水素油を精留塔５０に
注入して揮発油とディーゼル油の混合液を得、精留過程
を経てそれぞれ7.３kg、7.７kg、2.５kgの揮発油、ディ
ーゼル油、及び液化ガスを得ることができた。精留塔で
分離した揮発油とディーゼル油は悪臭及び汚染物の除去
によって、中国国家標識の７０番揮発油基準（ＧＢ４８
４−８９）と０番ディーゼル油基準（ＧＢ２５２−８
７）に符号する高品質の製品を得ることができた。特に
揮発油の場合、防爆性能に優れており、オクタン価が高
くて性質が安定である。尚、変質酸化性が全く無くて、
ネチネチしたり進展物が生じたりしないため、エンジン
のオイルパイプを支えさせるか或いはカーボンを蓄積さ
れることはない。The cracked and distilled hydrocarbon oil is injected into the rectification column 50 to obtain a mixed liquid of volatile oil and diesel oil, and 7.3 kg, 7.7 kg and 2.5 kg of volatile oil are obtained through the rectification process. , Diesel oil, and liquefied gas could be obtained. The volatile oil and diesel oil separated in the rectification tower were removed from the bad odor and pollutants, and the 70th volatile oil standard (GB48
4-89) and No. 0 diesel oil standard (GB252-8
We were able to obtain a high quality product that coded 7). Especially in the case of volatile oil, it has excellent explosion-proof performance, high octane number, and stable properties. In addition, there is no alteration oxidative property,
Since it does not graze or develop, it does not support the engine oil pipe or accumulate carbon.
【００２２】実施例２ 実施例１で行った方法に原料のみを、ポリスチレン、ポ
リエチレン、ポリプロピレン系廃プラスチックが重量比
で同量混合された切片に変えて触媒ＳｉＯ2 ＋Ａｌ2Ｏ
3 ＋Ａｌ2 （ＳｉＯ4 ）3 の存在の下で実施したとこ
ろ、それぞれ2.４kg、7.８kg、８kg、1.８kgのカーボン
ブラック、揮発油、ディーゼル油、液化ガスを得ること
ができ、最終精製された揮発油とディーゼル油の品質は
第１実施例の場合と差がなかった。 Example 2 A catalyst SiO 2 + Al 2 O was prepared by changing the raw material used in the method of Example 1 to a piece in which polystyrene, polyethylene and polypropylene waste plastic were mixed in equal weight ratios.
When carried out in the presence of 3 + Al 2 (SiO 4 ) 3 , 2.4 kg, 7.8 kg, 8 kg and 1.8 kg of carbon black, volatile oil, diesel oil and liquefied gas can be obtained, respectively. The quality of the refined volatile oil and diesel oil did not differ from that of the first embodiment.
【００２３】なお、上記に本発明の好ましい実施態様を
記載したが、当業者に対し明らかに教示される多くのこ
の発明の概念の変形及び／又は変更は、本発明の範囲に
含まれるものである。While the preferred embodiments of the invention have been described above, many variations and / or modifications of the inventive concept which will be apparently taught to those skilled in the art are intended to be within the scope of the invention. is there.
【００２４】[0024]
【発明の効果】このように本発明による装置及び方法を
使用すると、工程が簡単で操作が便利なので揮発油やデ
ィーゼル油などの燃料が容易に製造できる。更に、本発
明で用いる触媒の価格も低廉であって容易に購入するこ
とができ、全体的なシステム運営が簡単である。最も重
要なことは、硫黄のような公害物質が含まれていない良
質の燃料を製造して供給することができることである。As described above, when the apparatus and method according to the present invention are used, fuels such as volatile oil and diesel oil can be easily produced because the process is simple and the operation is convenient. Further, the catalyst used in the present invention is inexpensive and can be easily purchased, and the overall system operation is simple. Most importantly, it is capable of producing and supplying good quality fuels free of pollutants such as sulfur.
【００２５】勿論、本発明の方法によって石油も製造す
ることができるが、利用効率及び需要関係上、販路の有
利な揮発油とディーゼル油を主に製造した。上述したよ
うに、本発明は深刻な環境汚染源として台頭してきた石
油化学製品の廃プラスチック類を再び高品質の燃料に還
元させることにより、環境汚染の防止及びエネルギーの
再生産を図ることができる有用な効果を奏する。Of course, although petroleum can be produced by the method of the present invention, volatile oil and diesel oil, which are advantageous in sales channels, are mainly produced in terms of utilization efficiency and demand. As described above, the present invention is useful for preventing environmental pollution and recreating energy by returning waste plastics of petrochemical products, which have emerged as serious sources of environmental pollution, to high-quality fuel again. Has a great effect.
【図１】本発明の好ましい実施例による燃料製造装置の
全体概略図。FIG. 1 is an overall schematic view of a fuel manufacturing apparatus according to a preferred embodiment of the present invention.
【符号の説明】 １０ 原料供給装置 ２０ 螺旋形原料供給器 ２１ 駆動モータ ３０ クラッキングファーネス ４０ 加熱炉 ５０ 精留塔 ６０ 揮発油冷却器 ７０ ディーゼル油冷却器 ６１，７１ 冷却管 ６２，７２ ケース ６３，７３ 冷却水供給弁 ６４，７４ 排出管 ８０ 揮発油精製装置 ９０ ディーゼル油精製装置[Explanation of reference signs] 10 raw material supply device 20 spiral raw material supply device 21 drive motor 30 cracking furnace 40 heating furnace 50 rectification tower 60 volatile oil cooler 70 diesel oil cooler 61,71 cooling pipe 62,72 case 63,73 Cooling water supply valve 64,74 Discharge pipe 80 Volatile oil refiner 90 Diesel oil refiner
Claims (4)
グさせるクラッキングファーネスと、 前記クラッキングファーネスを加熱する加熱炉と、 前記クラッキングファーネスから生成された低沸点炭化
水素油を精留する精留塔と、 前記精留塔で精留された高温の揮発油を冷却する揮発油
冷却器と、 前記精留塔で精留された高温のディーゼル油を冷却する
ディ−ゼル油冷却器と、前記揮発油冷却器で冷却された
揮発油を精製する揮発油精製装置と前記ディーゼル油冷
却器で冷却されたディーゼル油を精製するディーゼル油
精製装置とを含む廃プラスチックを用いた燃料製造装
置。1. A raw material supply device, a spiral raw material supply device connected to the raw material supply device, a cracking furnace for cracking the raw material supplied from the spiral raw material supply device, and heating for heating the cracking furnace. Furnace, rectification column for rectifying low boiling point hydrocarbon oil produced from the cracking furnace, volatile oil cooler for cooling high temperature volatile oil rectified in the rectification column, and the rectification column A diesel oil cooler for cooling the high temperature diesel oil rectified in the above, a volatile oil refining device for refining the volatile oil cooled by the volatile oil cooler, and a diesel oil cooled by the diesel oil cooler A fuel production device using waste plastic, including a diesel oil refining device for refining.
と、 前記洗浄及び粉砕工程で設けられた原料をクラッキング
ファーネスまで供給する原料供給工程と、 触媒の存在下に原料を加熱して分解蒸留過程を経て低沸
点炭化水素油にクラッキングさせる分解蒸留工程と、 分解蒸留した低沸点炭化水素油を揮発油とディーゼル油
に分離する精留工程と、 前記精留された高温の揮発油とディーゼル油を冷却する
冷却工程と、冷却された揮発油とディーゼル油を精製す
る精製工程とを含んでなることを特徴とする廃プラスチ
ックを用いた燃料製造方法。2. A step of washing and pulverizing a raw material to be supplied, a raw material supplying step of supplying the raw material provided in the cleaning and pulverizing step to a cracking furnace, and a decomposition distillation process by heating the raw material in the presence of a catalyst. Cracking distillation step to crack low boiling point hydrocarbon oil through, rectification step to separate the cracked and distilled low boiling point hydrocarbon oil into volatile oil and diesel oil, the rectified high temperature volatile oil and diesel oil A method of producing fuel using waste plastic, comprising a cooling step of cooling and a refining step of refining the cooled volatile oil and diesel oil.
〜４５０℃であり、前記触媒がＳｉＯ2 ＋Ａｌ2Ｏ3 ＋
Ａｌ2 （ＳｉＯ4 ) 3 であることを特徴とする請求項２
記載の廃プラスチックを用いた燃料製造方法。3. The heating temperature in the decomposition distillation step is 350.
˜450 ° C. and the catalyst is SiO 2 + Al 2 O 3 +
Al 2 (SiO 4 ) 3 It is characterized by the above-mentioned.
A method for producing a fuel using the described waste plastic.
ン、及びポリスチレンのいずれか又はそれらの組み合わ
せからなる廃プラスチックを使用することを特徴とする
請求項２記載の廃プラスチックを用いた燃料製造方法。4. The method for producing a fuel using waste plastic according to claim 2, wherein the raw material is waste plastic made of any one of polyethylene, polypropylene, and polystyrene, or a combination thereof.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR19950056481 | 1995-12-26 | ||
| KR96-66845 | 1996-12-17 | ||
| KR1019960066845A KR0176743B1 (en) | 1995-12-26 | 1996-12-17 | Fuel manufacturing method and apparatus using waste plastic |
| KR95-56481 | 1996-12-17 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH09286991A true JPH09286991A (en) | 1997-11-04 |
Family
ID=26631522
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP34862896A Pending JPH09286991A (en) | 1995-12-26 | 1996-12-26 | Production of fuel using waste plastic and apparatus therefor |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JPH09286991A (en) |
| AU (1) | AU697420B2 (en) |
| ID (1) | ID18950A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100288731B1 (en) * | 1998-06-18 | 2001-05-02 | 김동춘 | Method for producing gasoline and diesel oil using waste vinyl and plastic waste, and apparatus |
| JP2021055026A (en) * | 2019-10-02 | 2021-04-08 | エムラボ株式会社 | Apparatus and method for converting organic matter into oil |
| WO2022144440A1 (en) * | 2020-12-31 | 2022-07-07 | Green Lizard Technologies Ltd | Production of carbon black |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112961698A (en) * | 2021-02-01 | 2021-06-15 | 中国计量大学 | Complete set of landfill waste plastic pyrolysis device and method |
-
1996
- 1996-12-23 ID ID963864A patent/ID18950A/en unknown
- 1996-12-24 AU AU76449/96A patent/AU697420B2/en not_active Ceased
- 1996-12-26 JP JP34862896A patent/JPH09286991A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100288731B1 (en) * | 1998-06-18 | 2001-05-02 | 김동춘 | Method for producing gasoline and diesel oil using waste vinyl and plastic waste, and apparatus |
| JP2021055026A (en) * | 2019-10-02 | 2021-04-08 | エムラボ株式会社 | Apparatus and method for converting organic matter into oil |
| WO2022144440A1 (en) * | 2020-12-31 | 2022-07-07 | Green Lizard Technologies Ltd | Production of carbon black |
Also Published As
| Publication number | Publication date |
|---|---|
| AU697420B2 (en) | 1998-10-08 |
| ID18950A (en) | 1998-05-28 |
| AU7644996A (en) | 1997-11-13 |
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