JP4323963B2 - Method for removing pyrolytic carbon from dry distillation gas of organic waste - Google Patents
Method for removing pyrolytic carbon from dry distillation gas of organic waste Download PDFInfo
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- 238000000197 pyrolysis Methods 0.000 title claims description 89
- 239000002296 pyrolytic carbon Substances 0.000 title claims description 48
- 238000000034 method Methods 0.000 title claims description 16
- 239000010815 organic waste Substances 0.000 title claims description 16
- 239000007789 gas Substances 0.000 claims description 79
- 238000001816 cooling Methods 0.000 claims description 33
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 17
- 229910052799 carbon Inorganic materials 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 14
- 238000002156 mixing Methods 0.000 claims description 3
- 239000002912 waste gas Substances 0.000 claims 1
- 239000003921 oil Substances 0.000 description 47
- 239000000295 fuel oil Substances 0.000 description 16
- 238000007664 blowing Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 239000010920 waste tyre Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000005661 hydrophobic surface Effects 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- 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
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- Processing Of Solid Wastes (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
本発明は、廃タイヤなどの有機系廃棄物をガス化処理する際に生成した乾留ガス中に含まれる熱分解カーボンを除去する方法に関するものである。 The present invention relates to a method for removing pyrolytic carbon contained in dry distillation gas generated when gasifying organic waste such as waste tires.
廃タイヤなどの有機系廃棄物を有効利用するために、有機系廃棄物を乾留して油分、ガスを回収して再利用することが提案されている。 In order to effectively use organic waste such as waste tires, it has been proposed to dry-distill organic waste, recover oil and gas, and reuse it.
例えば、特許文献１には、ゴム系廃棄物の熱分解工程で発生した熱分解ガスを冷却油に接触させて冷却して得られる精製ガスを熱分解工程の燃料として利用することが記載されている。 For example, Patent Document 1 describes that purified gas obtained by bringing a pyrolysis gas generated in a pyrolysis process of rubber waste into contact with cooling oil and cooling it is used as a fuel for the pyrolysis process. Yes.
なお未燃カーボンの除去に関連して、特許文献２には、燃焼排ガス中のＳＯＸと未燃カーボンの除去を目的として、脱硫吸収液と燃焼排ガスを気液接触させる際に、液中に入った未燃カーボンは除去されにくいことから、脱硫吸収液中に空気あるいは窒素ガスを吹き込んで形成した泡に未燃カーボンを付着させて脱硫吸収液から分離することが記載されている。
廃タイヤなどの有機系廃棄物を乾留する際、熱分解カーボンが乾留ガス中に随伴する。熱分解カーボンが乾留ガス中に含まれていると、後工程設備が詰まり閉塞による設備トラブルの原因になり、また、生成した乾留ガスから油分を回収して再利用するに際して、これら熱分解カーボンがエンジンの燃焼性能に悪影響を及ぼすことにもなる。 When organic waste such as waste tires are carbonized, pyrolytic carbon accompanies the carbonized gas. If pyrolytic carbon is contained in the dry distillation gas, it causes equipment troubles due to clogging of the post-process equipment, and when pyrolyzing carbon is recovered and reused, It will also adversely affect the combustion performance of the engine.
そこで、乾留ガス中からの熱分解カーボン除去をバグフィルタなどの集じん装置により行なおうとした場合、乾留ガス中の油分が液化し、集じん面に付着するため既存の集じん装置は使えない。また、単純に水による洗浄ということが考えられるが、水は表面張力が高いため何段にも洗浄する必要があり、また、ぬれ性を高めるために薬剤を用いる必要があるので、コストが高くなるという問題がある。 Therefore, when removing pyrolytic carbon from dry distillation gas using a dust collector such as a bag filter, the oil in the dry distillation gas liquefies and adheres to the dust collection surface, so the existing dust collector cannot be used. . In addition, it is possible to simply wash with water, but since water has a high surface tension, it is necessary to wash it in many stages, and it is necessary to use chemicals to improve wettability, so the cost is high. There is a problem of becoming.
なお、引用文献１には熱分解ガス中の未燃カーボンの除去については記載されてなく、
また、仮に引用文献２のように乾留ガスを吸収液に空気の吹込みで形成された泡で除去しようとすると、乾留ガスが燃焼して爆発するおそれがあるので危険であり、また、Ｎ２で気泡を形成すると、乾留ガスカロリーが下がり回収ガスの価値が下がる。
Reference 1 does not describe the removal of unburned carbon in the pyrolysis gas,
Further, if it is attempted to remove the dry distillation gas with bubbles formed by blowing air into the absorbing liquid as in the cited document 2, it is dangerous because the dry distillation gas may burn and explode, and N 2 If bubbles are formed, the dry calorie gas calorie decreases and the value of the recovered gas decreases.
そこで、本発明は、有機系廃棄物の乾留で生成した乾留ガス中から熱分解カーボンを高い除去率で且つ安全に除去して質のよい乾留ガスを得ることができる、有機系廃棄物の乾留ガスからの熱分解カーボン除去方法を提供するものである。 Therefore, the present invention provides a dry distillation of organic waste, which can obtain a high-quality dry distillation gas by safely removing pyrolytic carbon at a high removal rate from the dry distillation gas generated by the dry distillation of organic waste. A method for removing pyrolytic carbon from a gas is provided.
本発明は、有機系廃棄物の乾留により発生する乾留ガス中に含まれる熱分解カーボンを除去する方法において、熱分解カーボンを含む乾留ガスを冷却して回収油とする油分を液化する工程と、前記工程で液化した油分を密閉された貯留槽に回収油として貯留するとともに、貯留槽内の回収油中に冷却された前記乾留ガスを導入して回収油中に気泡を発生させて乾留ガス中の熱分解カーボンと回収油との固液混合により乾留ガス中の熱分解カーボンを回収油中に移行させて除去する工程と、熱分解カーボンが除去された乾留ガスを貯留槽の上部から抜き出す工程と、貯留槽の下部から回収油を抜き出し、固液分離装置にて熱分解カーボンを取り除いて油分を回収する工程と、貯留槽の上部から回収油を抜き出し、熱分解カーボンを含んだ乾留ガスの冷却油として循環させる工程とからなることを特徴とする。 The present invention relates to a method for removing pyrolytic carbon contained in a dry distillation gas generated by dry distillation of organic waste, a step of liquefying an oil component to be recovered oil by cooling the dry distillation gas containing the pyrolytic carbon, and The oil component liquefied in the above step is stored as recovered oil in a closed storage tank, and the dry distillation gas cooled in the recovered oil in the storage tank is introduced to generate bubbles in the recovered oil, thereby generating the dry distillation gas. The pyrolysis carbon in the dry distillation gas is transferred to the recovery oil by solid-liquid mixing of the pyrolysis carbon and the recovery oil, and the dry distillation gas from which the pyrolysis carbon has been removed is extracted from the upper part of the storage tank The recovered oil is extracted from the lower part of the storage tank, the pyrolysis carbon is removed by a solid-liquid separator, and the oil is recovered. The recovered oil is extracted from the upper part of the storage tank, and the dry distillation gas containing the pyrolytic carbon is collected. Characterized in that comprising the step of circulating a cooling oil.
本発明は、回収油として重質油を使用し、熱分解カーボン含有乾留ガスを吹き込み又は吸引により回収油中に導入して気泡を発生させて固液接触により熱分解カーボンを回収油に移行させるので、熱分解カーボンを高い除去効率で除去することができ、また、気泡の発生に空気やＮ２を用いないので安全であり且つ回収油のカロリーが低下することがない。 The present invention uses heavy oil as recovered oil, introduces pyrolytic carbon-containing dry distillation gas into the recovered oil by blowing or suction, generates bubbles, and transfers pyrolytic carbon to recovered oil by solid-liquid contact. Therefore, pyrolytic carbon can be removed with high removal efficiency, and since air and N 2 are not used for the generation of bubbles, it is safe and the calories of recovered oil do not decrease.
熱分解カーボンを含んだ乾留ガスを１２０〜１５０℃に冷却して液化した重質油を貯留槽の上部から抜き出して冷却油、媒体として循環使用させるので、設備的に極めて効率的であり、また、回収油が重質油であるため、循環冷媒とした場合、高温では低粘性、低比重となるため遠心分離機等での固液分離を効率良く行なって油分を回収することができる。 Since the heavy oil liquefied by cooling dry distillation gas containing pyrolytic carbon to 120-150 ° C is extracted from the upper part of the storage tank and circulated as cooling oil and medium, it is extremely efficient in terms of equipment. Since the recovered oil is a heavy oil, when it is used as a circulating refrigerant, it has a low viscosity and a low specific gravity at high temperatures. Therefore, the oil can be recovered by efficiently performing solid-liquid separation with a centrifugal separator or the like.
熱分解カーボンを含んだ乾留ガスは、１２０〜１５０℃に冷却して重質油分を液化する。冷却された乾留ガスを４９〜９８ｋＰａ（５０〜１００ｍｍＡｑ）の圧力で貯留槽内の回収油中に吹き込んで、又はＩＤＦ（吸引ファン）で、乾留ガスを−４９〜−９８ｋＰａ（−５０〜−１００ｍｍＡｑ）で吸引して、気泡を発生させる。分解カーボンを含んだ乾留ガスの冷却油としては、貯留槽の上部から抜き出した回収油を、８５〜９５℃に冷却して循環させる。回収油の固液分離は遠心分離機で実施する。 The dry distillation gas containing pyrolytic carbon is cooled to 120 to 150 ° C. to liquefy heavy oil. The cooled dry distillation gas was blown into the recovered oil in the storage tank at a pressure of 49 to 98 kPa (50 to 100 mmAq), or with IDF (suction fan), the dry distillation gas was -49 to -98 kPa (-50 to -100 mmAq). ) To generate bubbles. As the cooling oil for dry distillation gas containing cracked carbon, the recovered oil extracted from the upper part of the storage tank is cooled to 85 to 95 ° C. and circulated. Solid-liquid separation of recovered oil is performed with a centrifuge.
本発明において、乾留ガスを吹き込む又は吸引する冷却媒体には、疎水性表面を有する熱分解カーボンとの親和性を高めるため、極性の低い媒体で、低粘性、低比重であることが適することに着目した。即ち、これらは熱分解カーボンの遠心分離機能を効率的に確保するため及び、気泡による熱分解カーボンと溶媒の接触効率を高めるために是非必要であった。 In the present invention, the cooling medium for blowing or sucking dry distillation gas is suitable to be a low-polarity medium with low viscosity and low specific gravity in order to increase affinity with pyrolytic carbon having a hydrophobic surface. Pay attention. That is, they are necessary for efficiently ensuring the centrifugal separation function of pyrolytic carbon and for increasing the contact efficiency between pyrolytic carbon and solvent due to bubbles.
そのため、この溶媒として、熱分解カーボンを含んだ乾留ガスを１２０゜〜１５０℃に冷却して得られた液化重質油が最適であることを知見し完成したものである。 Therefore, the present inventors have found out that a liquefied heavy oil obtained by cooling a dry distillation gas containing pyrolytic carbon to 120 ° to 150 ° C. is optimal as this solvent.
図１は本発明による乾留ガス中から熱分解カーボンを除去する一実施例のフローを示す図である。 FIG. 1 is a diagram showing a flow of one embodiment for removing pyrolytic carbon from the dry distillation gas according to the present invention.
廃タイヤ、ゴムホースなどの有機系廃棄物を密閉状態にあるロータリーキルン１に装入し、加熱して乾留する。乾留により熱分解して乾留ガスと、熱分解カーボンや廃棄物中のワイヤなどの残渣が得られる。 Organic waste such as waste tires and rubber hoses are charged into the rotary kiln 1 in a sealed state and heated to dry distillation. Pyrolysis gas and pyrolysis carbon and residues such as wires in waste are obtained by pyrolysis by dry distillation.
ロータリーキルン１から排出した乾留ガスは、熱分解カーボンを随伴しているため、乾留ガス中から熱分解カーボンを除去する工程へ送られる。まず、ロータリーキルン１から排出した乾留ガスは、貯留槽４の乾留ガスをＩＤＦ（吸引ファン）２により吸引して冷却装置３へ導入する。あるいは、図１の点線で示す加圧ポンプ２ａで加圧して冷却装置３へ圧送しても良い。
Since the dry distillation gas discharged from the rotary kiln 1 is accompanied by pyrolytic carbon, it is sent to the step of removing the pyrolytic carbon from the dry distillation gas. First, the dry distillation gas discharged from the rotary kiln 1 sucks the dry distillation gas in the storage tank 4 with an IDF (suction fan) 2 and introduces it into the cooling device 3. Or you may pressurize with the
冷却装置３へ導入された乾留ガスは、約５５０℃から約１２０〜１５０℃に冷却される。冷却装置３での乾留ガスの冷却は、冷却装置内の上部から冷却油として貯留槽４から循環ポンプ５で送られてくる回収油をスプレーして行う。この冷却により、乾留ガスが冷却されて乾留ガス中の沸点が約１２０〜１５０℃以上の重質油分が液化する。 The dry distillation gas introduced into the cooling device 3 is cooled from about 550 ° C. to about 120 to 150 ° C. Cooling of the dry distillation gas in the cooling device 3 is performed by spraying the recovered oil sent from the storage tank 4 by the circulation pump 5 as cooling oil from the upper part in the cooling device. By this cooling, the dry distillation gas is cooled and a heavy oil component having a boiling point in the dry distillation gas of about 120 to 150 ° C. or more is liquefied.
冷却装置３の下部には密閉された貯留槽４が配置され、冷却装置内を下降した熱分解カーボンを含有した乾留ガスが吹き出す筒状の乾留ガス吹出し口３ａが冷却装置３の下部に設けられ、乾留ガス吹出し口３ａは貯留槽４に貯留されている重質油からなる回収油６に浸漬させておく。 A sealed storage tank 4 is arranged at the lower part of the cooling device 3, and a cylindrical dry distillation gas outlet 3 a through which dry distillation gas containing pyrolytic carbon descending the cooling device blows out is provided at the lower part of the cooling device 3. The dry distillation gas outlet 3 a is immersed in the recovered oil 6 made of heavy oil stored in the storage tank 4.
乾留ガス吹出し口３ａを回収油６へ浸漬させておくことによって、熱分解カーボンを含有した乾留ガスは、吸引あるいは加圧により気泡７を発生させながら回収油６へ導入される。乾留ガスを吸引により導入する場合は例えば約５０〜１００ｍｍの深さで約−１ｋＰａ程度、乾留ガスを加圧により導入する場合は、圧損を考慮して、例えば約５０〜１００ｍｍの深さで約１ｋＰａ程度とする。気泡７は、熱分解カーボンと回収油６との接触効率を高めて固液混合を促進させるために小さい気泡を多く発生させるのがよい。本発明では、回収油６が粘性の低い且つ比重の小さい重質油なので、乾留ガスの吹込により回収油６の中に気泡７が発生し易く、気泡により乾留ガス中の熱分解カーボンが気泡７に捕捉されて回収油６の中に移行して行き、熱分解カーボンの除去率を向上させることができる。 By immersing the dry distillation gas outlet 3a in the recovered oil 6, the dry distillation gas containing pyrolytic carbon is introduced into the recovered oil 6 while generating bubbles 7 by suction or pressurization. When introducing dry distillation gas by suction, for example, about -1 kPa at a depth of about 50 to 100 mm, and when introducing dry distillation gas by pressurization, considering pressure loss, for example, at a depth of about 50 to 100 mm. It is about 1 kPa. The bubbles 7 should preferably generate many small bubbles in order to increase the contact efficiency between the pyrolytic carbon and the recovered oil 6 and promote solid-liquid mixing. In the present invention, since the recovered oil 6 is a heavy oil having a low viscosity and a small specific gravity, bubbles 7 are easily generated in the recovered oil 6 by blowing dry distillation gas, and the pyrolytic carbon in the dry distillation gas is generated by the bubbles. It can be captured by the gas and transferred into the recovered oil 6 to improve the removal rate of pyrolytic carbon.
また、乾留ガス吹出し口３ａの浸漬によって冷却装置３の内部と貯留槽４の回収油上の空間が遮断されているので、冷却装置内の熱分解カーボンが熱分解カーボンを除去した貯留槽４の揮発分に移行することがないので、きれいな乾留ガスが得られる。 Further, since the interior of the cooling device 3 and the space above the recovered oil in the storage tank 4 are blocked by the immersion of the dry distillation gas outlet 3a, the pyrolysis carbon in the cooling apparatus removes the pyrolysis carbon from the storage tank 4. Since it does not shift to volatile matter, clean dry distillation gas can be obtained.
なお、気泡を発生させるために冷却装置３の乾留ガス吹出し口３ａを重質油中に浸漬した状態にしておく必要があるので、操業開始にあたっては、貯留槽４に予め重質油を一定レベルまで貯留して乾留ガス吹出し口３ａを重質油中に浸漬しておく。 In order to generate bubbles, it is necessary to keep the dry distillation gas outlet 3a of the cooling device 3 immersed in heavy oil. Therefore, at the start of operation, a certain level of heavy oil is stored in the storage tank 4 in advance. Until the dry distillation gas outlet 3a is immersed in heavy oil.
冷却装置３で液化した重質油分は、回収油６として貯留槽４に貯留されるが、貯留槽４の回収油６は循環ポンプ５により冷却装置３に冷却油として循環させる。冷却装置３へ循環させる回収油は、貯留槽４では重質油分の沸点が約１２０〜１５０℃程度の温度なので、このまま冷却油にしてもロータリーキルン１から冷却装置３に導入される約５５０℃の高温乾留ガスを冷却装置３の出口で１２０〜１５０℃に冷却させるため、冷却装置３の入口では約８８℃となるように熱交換器８で冷却される。 The heavy oil liquefied by the cooling device 3 is stored in the storage tank 4 as the recovered oil 6, but the recovered oil 6 in the storage tank 4 is circulated to the cooling apparatus 3 by the circulation pump 5 as the cooling oil. The recovered oil to be circulated to the cooling device 3 has a boiling point of about 120 to 150 ° C. in the storage tank 4, so that the boiling point of the heavy oil is about 550 ° C. introduced into the cooling device 3 from the rotary kiln 1. In order to cool the high-temperature dry distillation gas to 120 to 150 ° C. at the outlet of the cooling device 3, it is cooled by the heat exchanger 8 so as to be about 88 ° C. at the inlet of the cooling device 3.
貯留槽４に貯留される回収油６は、ポンプ１０で抜き出して固液分離装置として遠心分離機９を用いて熱分解カーボンと重質油分に分離し、回収した油分は貯槽１１に貯留し、冷却装置３で液化される重質油相当分は再生油として回収する。回収した重質油分の一部はポンプ１２で貯留槽４へ戻し、貯留槽内で一定レベルの油量を維持させるとともに、回収油６に移行した熱分解カーボンが蓄積するのを防止する。
The recovered oil 6 stored in the storage tank 4 is extracted by a
貯留槽４では、熱分解カーボンが除去された沸点の低い軽質油分を含む乾留ガスとして貯留槽４の上部から抜き出して精製乾留ガスとして回収し、次工程で沸点差を利用して各種の油分を回収する。 In the storage tank 4, it is extracted from the upper part of the storage tank 4 as a dry distillation gas containing a light oil component having a low boiling point from which pyrolytic carbon has been removed, and is recovered as a purified dry distillation gas. to recover.
以上の構成において、ロータリーキルンから排出された、熱分解カーボンを約５４ｋｇ／ｈ含有した乾留ガスを、本発明の方法により処理した結果、熱分解カーボンを約５．４ｋｇ／ｈ含有した乾留ガスまで熱分解カーボンを除去することができた。 In the above configuration, the dry distillation gas containing about 54 kg / h of pyrolytic carbon discharged from the rotary kiln was processed by the method of the present invention. As a result, the dry distillation gas containing about 5.4 kg / h of pyrolytic carbon was heated. Decomposed carbon could be removed.
１：ロータリーキルン
２：ＩＤＦ（吸引ファン）
２ａ：加圧ポンプ
３：冷却装置
３ａ：乾留ガス吹出し口
４：貯留槽
５：循環ポンプ
６：回収油
７：気泡
８：熱交換器
９：遠心分離機
１０：ポンプ
１１：貯槽
１２：ポンプ
1: Rotary kiln 2: IDF (suction fan)
2a: pressurizing pump 3: cooling device 3a: dry distillation gas outlet 4: storage tank 5: circulation pump 6: recovered oil 7: bubbles 8: heat exchanger 9: centrifuge 10: pump 11: storage tank 12: pump
Claims (6)
熱分解カーボンを含む乾留ガスを冷却装置にて冷却して回収油とする油分を液化する工程と、
前記工程で液化した油分を密閉された貯留槽に回収油として貯留するとともに、貯留槽内の回収油中に冷却された熱分解カーボンを含む乾留ガスを導入して回収油中に気泡を発生させて乾留ガス中の熱分解カーボンと回収油との固液混合により乾留ガス中の熱分解カーボンを回収油中に移動させて除去する工程と、
熱分解カーボンが除去された乾留ガスを貯留槽の上部から抜き出す工程と、
貯留槽の下部から回収油を抜き出し、固液分離装置にて熱分解カーボンを取り除いて油分を回収する工程と、
貯留槽の上部から回収油を抜き出し、熱分解カーボンを含んだ乾留ガスの冷却油として循環させる工程とからなることを特徴とする有機系廃棄物の乾留ガスからの熱分解カーボン除去方法。 In a method for removing pyrolytic carbon contained in dry distillation gas generated by dry distillation of organic waste,
A step of liquefying oil to be recovered oil by cooling dry distillation gas containing pyrolytic carbon with a cooling device;
The oil liquefied in the above process is stored as recovered oil in a sealed storage tank, and a dry distillation gas containing pyrolytic carbon cooled in the recovered oil in the storage tank is introduced to generate bubbles in the recovered oil. Removing the pyrolytic carbon in the dry distillation gas by moving it into the recovered oil by solid-liquid mixing of the pyrolytic carbon in the dry distillation gas and the recovered oil;
Extracting the dry distillation gas from which pyrolytic carbon has been removed from the upper part of the storage tank;
Extracting the recovered oil from the lower part of the storage tank, removing the pyrolytic carbon in a solid-liquid separator, and recovering the oil;
A method for removing pyrolytic carbon from a dry distillation gas of organic waste, comprising the step of extracting the recovered oil from the upper part of the storage tank and circulating it as a cooling oil for the dry distillation gas containing pyrolytic carbon.
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| CN103131453B (en) * | 2013-03-11 | 2015-07-01 | 北京神雾环境能源科技集团股份有限公司 | Pyrolytic evaluation device for carbon-containing substances |
| CN103203169B (en) * | 2013-03-28 | 2015-04-15 | 黄楚铭 | Continuous and zero-emission organic waste processing and recycling system |
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| JP2023023316A (en) * | 2021-08-05 | 2023-02-16 | 荏原環境プラント株式会社 | Treatment apparatus and treatment method for recovering decomposition oil from pyrolysis gas |
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