JP6914539B2

JP6914539B2 - Methods and equipment for separating solids from fluidized beds

Info

Publication number: JP6914539B2
Application number: JP2018504399A
Authority: JP
Inventors: 斉井上
Original assignee: Individual
Current assignee: Individual
Priority date: 2016-03-07
Filing date: 2017-02-28
Publication date: 2021-08-04
Anticipated expiration: 2037-02-28
Also published as: WO2017154679A1; JPWO2017154679A1

Description

本発明は、流動層から固形物を効果的に分離する方法および装置に関するものである。 The present invention relates to methods and devices for effectively separating solids from a fluidized bed.

更に具体的には、本発明は、流動層内に存在する、流動媒体よりも粒径が大きく、且つ、粒子密度の小さい固形物を分離する方法および装置を提供するものである。本発明による方法および装置によると、例えば、バイオマスの流動層ガス化装置において、ガスとともに副生するチャーを、流動媒体と分離して抜出した上で土壌還元し、再生可能エネルギーを生産するとともに、炭素固定による大気中の二酸化炭素濃度の増大抑制およびバイオマスの持続可能な生産を図ることが可能となる。またそれにとどまらず、流動媒体より粒径が大きく、且つ、粒子密度の小さい固形物を除去する他の用途にも応用が可能である。 More specifically, the present invention provides a method and an apparatus for separating a solid substance having a larger particle size and a smaller particle density than a flow medium existing in a fluidized bed. According to the method and apparatus according to the present invention, for example, in a fluidized bed gasification apparatus for biomass, char produced as a by-product with gas is separated from the fluidized medium and extracted, and then reduced to soil to produce renewable energy. It is possible to suppress the increase in carbon dioxide concentration in the atmosphere by carbon fixation and to achieve sustainable production of biomass. In addition to that, it can be applied to other applications for removing solid matter having a larger particle size and a smaller particle density than a fluid medium.

近年、地球の温暖化を防止し、また、石炭や石油などの有限な化石燃料資源の枯渇を避けるため、再生可能な自然エネルギー利用技術を開発し、それを広範に普及させることが世界的な緊急課題となっている。自然エネルギーの中でも特にバイオマスエネルギーは、賦存量が大きく、また燃料への転換が比較的容易であることなどから、自然エネルギーの筆頭と位置付けられることが多い。 In recent years, in order to prevent global warming and avoid the depletion of finite fossil fuel resources such as coal and oil, it is worldwide to develop and widely disseminate renewable renewable energy utilization technology. It is an urgent issue. Among natural energies, biomass energy is often regarded as the leading natural energy because of its large endowment and relatively easy conversion to fuel.

バイオマスのエネルギー利用技術には、直接燃焼、熱化学的変換技術、生化学的変換技術があるが、直接燃焼は特に小規模プロセスの場合効率に限界があり、また生化学的変換では、糖質やでんぷん質などの限られたバイオマスしか原料にできないという問題がある。一方、熱化学的変換によれば、セルロース系化合物を含め、バイオマスを全体として利用でき、かつ小規模でも高効率のエネルギー利用が可能となる。 Biomass energy utilization technologies include direct combustion, thermochemical conversion technology, and biochemical conversion technology, but direct combustion has limited efficiency, especially in small-scale processes, and in biochemical conversion, sugars. There is a problem that only limited biomass such as starch can be used as a raw material. On the other hand, according to the thermochemical conversion, biomass including cellulosic compounds can be used as a whole, and energy can be used with high efficiency even on a small scale.

しかし、既存の熱化学的変換技術においては、無触媒のガス化は、低温ではタールが生成するため、高温にする必要があり、装置材料の熱的負担の増加と熱効率の低下がさけられない。また、ガス化剤の一部または全部として空気を用いて部分燃焼させる方式では、生成ガスが低発熱量・低品質のガスとなる。それを避けるためにガス化剤をスチームのみとした外熱式のガス化炉を用いることが提案されているが、このような外燃式ガス化炉は熱効率が低く、また熱伝達の問題から、規模や構造にも制約がある。触媒を用いた場合、ガス化温度を下げることはできるものの、一般に触媒は高価であり、またすみやかに劣化ないし失活してしまう、という問題があった。 However, in the existing thermochemical conversion technology, in the non-catalytic gasification, tar is generated at a low temperature, so that it is necessary to raise the temperature, which inevitably increases the thermal load on the equipment material and reduces the thermal efficiency. .. Further, in the method of partially combusting using air as a part or all of the gasifying agent, the generated gas becomes a gas having a low calorific value and low quality. In order to avoid this, it has been proposed to use an external heat type gasifier that uses only steam as the gasifying agent, but such an external combustion type gasifier has low thermal efficiency and has problems with heat transfer. , There are also restrictions on scale and structure. When a catalyst is used, although the gasification temperature can be lowered, there is a problem that the catalyst is generally expensive and is quickly deteriorated or deactivated.

これらの問題を解決するべく、既に本発明者らは、バイオマスを含む有機物系原料を、ガス化反応ゾーンにおいて、昇温条件下、ガス化剤の存在下において、触媒機能および/または熱媒体機能を有する粘土からなるガス化促進剤と流動接触させることによって、前記有機物系原料を気体・液体燃料製造のための有用ガスに転換する技術を開発している(特許文献１：特許第４２５９７７７号)。この技術によれば、４００℃〜７５０℃の比較的温和な温度条件下において、タールの生成を抑制しつつ、有機物系原料を効率的にガス化することができる。 In order to solve these problems, the present inventors have already put organic raw materials containing biomass into a gasification reaction zone, under heating conditions, and in the presence of a gasifying agent, as a catalytic function and / or a heat medium function. We are developing a technique for converting the organic raw material into a useful gas for producing gas / liquid fuel by making fluid contact with a gasification accelerator made of clay (Patent Document 1: Patent No. 4259777). .. According to this technique, it is possible to efficiently gasify an organic raw material while suppressing the formation of tar under relatively mild temperature conditions of 400 ° C. to 750 ° C.

さらに本発明者は、そのような技術において、ガス化反応ゾーンと再生ゾーンとの隔壁として金属等の熱伝達性の高い材料を用いることによって、再生ゾーンからガス化反応ゾーンへの放射、伝導ならびに対流による熱伝達を行い、前記熱伝達がない場合と比べて再生ゾーンの温度を低減することができ、かつ装置の自動温度調整機能を高めることができることを特徴とするバイオマスのガス化方法を開発している(特許文献２：特許第４５４９９１８号）。 Furthermore, in such a technique, the present inventor uses a material having high heat transferability such as metal as a partition wall between the gasification reaction zone and the regeneration zone, so that radiation, conduction from the regeneration zone to the gasification reaction zone, and conduction can be achieved. Developed a biomass gasification method characterized by performing heat transfer by convection, reducing the temperature of the regeneration zone as compared with the case without the heat transfer, and enhancing the automatic temperature adjustment function of the device. (Patent Document 2: Patent No. 4549918).

一般に、バイオマスをガス化する際、原料のバイオマスのサイズが大きいと、バイオマス内部の昇温速度が小さくなり、タールの発生が増大するという問題があるため、一般には、ガス化装置に投入するに先立ち、バイオマスを細かく粉砕する必要がある。 Generally, when gasifying biomass, if the size of the raw material biomass is large, there is a problem that the rate of temperature rise inside the biomass decreases and tar generation increases. Prior to this, it is necessary to crush the biomass into small pieces.

この点において、本発明者の前述の発明による、触媒機能および/または熱媒体機能を有する粘土粒子をガス化促進剤と流動接触させることによってガス化する方法では、粘土が投入されたバイオマスを包囲して、発生したタールを吸着・分解することから、未粉砕のバイオマスを、そのまま投入できる利点がある。また、該発明において触媒として利用する粘土粒子のせん断応力が小さいため、投入したバイオマスとほぼ同様の形状をした、大型のチャーが得られる。 In this respect, the method of gasifying clay particles having a catalytic function and / or a heat medium function by fluid contact with a gasification accelerator according to the above-mentioned invention of the present inventor surrounds the biomass into which the clay is charged. Then, since the generated tar is adsorbed and decomposed, there is an advantage that uncrushed biomass can be input as it is. Further, since the shear stress of the clay particles used as the catalyst in the present invention is small, a large-sized char having almost the same shape as the added biomass can be obtained.

このチャーを流動層から分離して抜出し土壌還元すれば、それだけ地球温暖化の原因である炭素を固定することになる。また、チャーは、バイオマスに由来するミネラルに富み、チッソ固定菌等の有用な微生物の繁殖を促し、さらに土壌の透水性・保水性を改善することから、土壌改良効果が大きく、植物の持続的な生育を助けることにもなる。すなわち、再生可能エネルギーの生産とともに、炭素固定と、植物の持続可能な生産をはかれることになる。伝統的な炭焼き工程から得られる炭も従来より土壌改良のために用いられてきたが、そのような伝統的な炭焼きでは、炭を生成する際に発生するエネルギー（有用ガス）を廃棄している。したがって、この点においても上述した先行発明は、いずれも発生したエネルギー（有用ガス）を発電に利用することができる点で、まさにバイオマス資源を余すところなく利用するものである。 If this char is separated from the fluidized bed and extracted and reduced to soil, carbon, which is the cause of global warming, will be fixed. In addition, char is rich in minerals derived from biomass, promotes the growth of useful microorganisms such as nitrogen-fixing bacteria, and further improves soil permeability and water retention, so it has a large soil improvement effect and sustains plants. It also helps the growth. In other words, along with the production of renewable energy, carbon fixation and sustainable production of plants will be promoted. Charcoal obtained from the traditional charcoal burning process has also been used for soil improvement in the past, but in such traditional charcoal burning, the energy (useful gas) generated when producing charcoal is discarded. .. Therefore, in this respect as well, the above-mentioned prior inventions all utilize the generated energy (useful gas) for power generation, and thus fully utilize the biomass resources.

このようにバイオマスのエネルギー利用の副産物としてのチャーを有効に利用するためには、流動層から固形物であるチャーを抜き出す方法が必要となる。従来の、流動層から固形物を抜き出す方法としては、特開２００４−１３８３７８「不燃物抜出システムおよび流動層炉システム」（特許文献３）や特開平０８−０２８８４２「流動層ごみ焼却炉における不燃物排出方法及び装置」（特許文献４）などが提案されているが、これらの技術はいずれも、流動層の炉底に沈み込む、流動媒体より粒子密度の大きい固形物を抜き出しの対象としている。バイオマス由来のチャーのように、粒子密度が比較的小さく、気泡流動層の濃厚相上部に浮遊して存在する固形物を効果的に分離する技術はいまだ開発されていない。 In order to effectively utilize char as a by-product of biomass energy utilization, a method of extracting solid char from the fluidized bed is required. Conventional methods for extracting solid matter from a fluidized bed include Japanese Patent Application Laid-Open No. 2004-138378 “Incombustible Material Extraction System and Fluidized Bed Reactor System” (Patent Document 3) and Japanese Patent Application Laid-Open No. 08-028842 “Incombustible in Fluidized Bed Waste Incinerator”. "Material discharge methods and devices" (Patent Document 4) have been proposed, but all of these technologies target solid materials having a particle density higher than that of the fluidized bed, which sink into the bottom of the fluidized bed. .. A technique for effectively separating solids having a relatively low particle density and floating above the dense phase of a bubble fluidized bed, such as biomass-derived char, has not yet been developed.

登録特許第４２５９７７７号Registered Patent No. 4259777 登録特許第４５４９９１８号Registered Patent No. 4549918 特開２００４−１３８３７８号Japanese Unexamined Patent Publication No. 2004-138378 特開平０８−０２８８４２号Japanese Patent Application Laid-Open No. 08-028842

本発明は、上述の技術的課題を解決するためのものであり、特に、流動媒体を構成する物質の径と、分離対象となる流動層内の固形物の径が異なる場合に、気泡流動層から、当該固形物を効果的に分離し回収する方法ならびに装置を提供する。 The present invention is for solving the above-mentioned technical problems, and particularly when the diameter of the substance constituting the fluidized medium and the diameter of the solid substance in the fluidized bed to be separated are different, the bubble fluidized bed. To provide a method and an apparatus for effectively separating and recovering the solid matter.

上述した技術的課題を解決するために、本発明に係る固形物の回収方法は、流動層内に存在する比較的粗大な固形物を、流動媒体から分離し流動層装置外に連続的に搬出する方法であって、前記固形物の径より小さく前記流動層の流動媒体をなす物質の径より大きい間隙であって、前記流動媒体が通過しかつ前記固形物が選択的に捕捉される径の間隙を多数持った捕捉帯を有する帯状搬送手段の一部を前記流動層装置内に設置し、連続的に循環させることによって、前記固形物を流動層装置外に連続的に分離し搬出するようにしたことを特徴としている。ここで、捕捉帯とは、前記固形物を捕捉する帯状機構のことをいい、帯状搬送手段の搬送面と一体化して設けることができる。 In order to solve the above-mentioned technical problems, the solid matter recovery method according to the present invention separates the relatively coarse solid matter existing in the fluidized bed from the fluidized bed and continuously carries it out of the fluidized bed apparatus. A gap having a diameter smaller than the diameter of the solid matter and larger than the diameter of the substance forming the fluidized bed of the fluidized bed, which is a diameter through which the fluidized bed passes and the solid matter is selectively captured. A part of the strip-shaped transport means having a trapping zone having a large number of gaps is installed in the fluidized bed device and continuously circulated so that the solid matter is continuously separated and carried out of the fluidized bed device. It is characterized by the fact that it was made. Here, the trapping band refers to a band-shaped mechanism for catching the solid matter, and can be provided integrally with the transport surface of the strip-shaped transport means.

本発明の好ましい態様においては、上記流動層が気泡流動層からなる。 In a preferred embodiment of the present invention, the fluidized bed is composed of a bubble fluidized bed.

更に、本発明の好ましい態様においては、上記帯状搬送手段がベルト状のコンベアからなり、該帯状搬送手段は、前記流動層の濃厚相部上端付近を一定区間水平に移動するようにすることが好ましい。 Further, in a preferred embodiment of the present invention, it is preferable that the strip-shaped transport means comprises a belt-shaped conveyor, and the strip-shaped transport means horizontally moves in the vicinity of the upper end of the concentrated phase portion of the fluidized bed in a certain section. ..

また、本発明においては、前記流動層内において、前記帯状搬送手段が配置される位置の流動層の空塔速度とそれ以外の流動層部位の空塔速度に差異をつけることによって、前記固形物が前記帯状搬送手段の捕捉面に誘導されるようにすることが好ましい。 Further, in the present invention, the solid matter is formed by making a difference between the superficial velocity of the fluidized bed at the position where the strip-shaped transport means is arranged and the superficial velocity of the other fluidized bed portion in the fluidized bed. Is preferably guided to the trapping surface of the strip-shaped transport means.

また、本発明の他の好ましい態様においては、前記帯状搬送手段は、前記捕捉帯に代わり、前記固形物の分離・回収用のコレクターを備えていてもよい。該コレクターは複数の刃を備え、該刃の間隔は、該固形物の径より小さく前記流動層の流動媒体をなす物質の径より大きい。該コレクターは、該帯状搬送手段に、固形物を捕捉可能な態様で、複数個備えられることが好ましい。本発明において、該帯状搬送手段が配置された位置の流動層付近に誘導された固形物が該コレクターにより捕捉され、該捕捉された固形物が、該帯状搬送手段と該コレクターの循環運動にともない流動層から掻き上げられ、ついで流動層装置外に連続的に分離・搬出されることが好ましい。 Further, in another preferred embodiment of the present invention, the band-shaped transport means may include a collector for separating / recovering the solid matter in place of the trapping band. The collector comprises a plurality of blades, the distance between the blades being smaller than the diameter of the solid and larger than the diameter of the material forming the fluidized bed of the fluidized bed. It is preferable that the strip-shaped transport means is provided with a plurality of collectors in a manner capable of capturing solid matter. In the present invention, the solid matter induced near the fluidized bed at the position where the strip-shaped transport means is arranged is captured by the collector, and the trapped solid matter accompanies the circulating motion of the strip-shaped transport means and the collector. It is preferable that the material is scraped up from the fluidized bed and then continuously separated and carried out of the fluidized bed device.

さらにまた、本発明の好ましい態様においては、上記方法が、バイオマスの流動層ガス化プロセスに導入される。 Furthermore, in a preferred embodiment of the invention, the method is introduced into the fluidized bed gasification process of biomass.

なお、本発明においては、分離対象である前記固形物は、通常の場合、バイオマス由来のチャーからなる。 In the present invention, the solid matter to be separated usually consists of biomass-derived char.

一方、本発明に係る装置は、流動層内に存在する比較的粗大な固形物を、流動媒体から分離し流動層装置外に連続的に搬出するための装置であって、前記固形物の径より小さく前記流動層の流動媒体をなす物質の径より大きい間隙であって、前記流動媒体が通過しかつ前記固形物が選択的に捕捉される径の間隙を多数持つ捕捉帯を有する帯状搬送手段と、前記帯状搬送手段の一部を前記流動層装置内に導入し、連続的に循環させるための動力手段とを有し、前記帯状搬送手段によって選択的に捕捉された前記固形物を流動層装置外に連続的に分離し搬出するようにしたことを特徴としている。 On the other hand, the apparatus according to the present invention is an apparatus for separating a relatively coarse solid matter existing in the fluidized bed from the fluidized bed and continuously carrying it out of the fluidized bed apparatus, and has a diameter of the solid matter. A strip-shaped transport means having a smaller gap larger than the diameter of the material forming the fluidized bed of the fluidized bed, and having a large number of gaps having a diameter through which the fluidized bed passes and the solid matter is selectively trapped. And a power means for introducing a part of the strip-shaped transport means into the fluidized bed device and continuously circulating the strip-shaped transport means, and the solid matter selectively captured by the strip-shaped transport means in the fluidized bed. It is characterized by being continuously separated and carried out of the device.

上記本発明に係る装置において、前記流動層は、好ましくは気泡流動層である。 In the apparatus according to the present invention, the fluidized bed is preferably a bubble fluidized bed.

さらに、本発明に係る装置の好ましい態様においては、前記帯状搬送手段がベルト状のコンベアからなり、さらに該帯状搬送手段が、前記流動層の濃厚相部上端付近を一定区間水平に移動するように設けられていることが好ましい。また、そのようなベルト状のコンベアの例として、チェーンコンベアを用いることができる。 Further, in a preferred embodiment of the apparatus according to the present invention, the strip-shaped transport means comprises a belt-shaped conveyor, and the strip-shaped transport means moves horizontally in the vicinity of the upper end of the concentrated phase portion of the fluidized bed for a certain section. It is preferable that it is provided. Further, as an example of such a belt-shaped conveyor, a chain conveyor can be used.

さらに本発明に係る装置においては、前記流動層内において、前記帯状搬送手段が配置される位置の流動層の空塔速度とそれ以外の流動層部位の空塔速度に差異をつける装置をさらに具備し、前記固形物が前記帯状搬送手段の捕捉面に誘導されるようにすることが好ましい。 Further, the apparatus according to the present invention further includes an apparatus for making a difference between the superficial velocity of the fluidized bed at the position where the strip-shaped transport means is arranged and the superficial velocity of the other fluidized bed portion in the fluidized bed. It is preferable that the solid matter is guided to the trapping surface of the strip-shaped transport means.

また、本発明に係る他の好ましい態様の装置においては、前記帯状搬送手段は、前記捕捉帯に代わり、前記固形物の分離・回収用のコレクターを備えていてもよい。該コレクターは複数の刃を備え、該刃の間隔は、該固形物の径より小さく前記流動層の流動媒体をなす物質の径より大きい。該コレクターは、該帯状搬送手段に、固形物を捕捉可能な態様で、複数個備えられることが好ましい。本発明において、該帯状搬送手段が配置された位置の流動層付近に誘導された固形物が、該コレクターにより捕捉され、該帯状搬送手段と該コレクターの循環運動にともない流動層から掻き上げられ、ついで流動層装置外に連続的に分離・搬出されることが好ましい。 Further, in the device of another preferred embodiment according to the present invention, the band-shaped transport means may include a collector for separating / recovering the solid matter in place of the trapping band. The collector comprises a plurality of blades, the distance between the blades being smaller than the diameter of the solid and larger than the diameter of the material forming the fluidized bed of the fluidized bed. It is preferable that the strip-shaped transport means is provided with a plurality of collectors in a manner capable of capturing solid matter. In the present invention, the solid matter induced near the fluidized bed at the position where the strip-shaped transport means is arranged is captured by the collector and is scraped up from the fluidized bed as the strip-shaped transport means and the collector circulate. Then, it is preferable that the fluidized bed device is continuously separated and carried out of the fluidized bed device.

また、本発明に係る固形物回収装置は、バイオマスの流動層ガス化装置に導入ないし組み込まれることが好ましい。 Further, the solid matter recovery device according to the present invention is preferably introduced or incorporated into a fluidized bed gasification device for biomass.

なお、本発明に係る装置による分離対象である前記固形物は、通常の場合、バイオマス由来のチャーからなる。 The solid substance to be separated by the apparatus according to the present invention usually consists of biomass-derived char.

上記の本発明に係る固形物の回収技術は、たとえば本発明者が既に開発したバイオマスのガス化技術に好適に適用され得る。たとえば、前述した特許文献１（特許第４２５９７７７号)に記載のバイオマスのガス化技術においては、バイオマスを含む有機物系原料を、ガス化反応ゾーンにおいて、昇温条件下、ガス化剤の存在下において、触媒機能および/または熱媒体機能を有する粘土からなるガス化促進剤と流動接触させることによって、前記有機物系原料を気体・液体燃料製造のための有用ガスに転換され、この技術によれば、４００℃〜７５０℃の比較的温和な温度条件下において、タールの生成をともなうことなく、有機物系原料を効率的にガス化することができる。 The above-mentioned solid matter recovery technique according to the present invention can be suitably applied to, for example, the biomass gasification technique already developed by the present inventor. For example, in the biomass gasification technique described in Patent Document 1 (Patent No. 4259777) described above, an organic raw material containing biomass is used in a gasification reaction zone under heating conditions and in the presence of a gasifying agent. By fluid contact with a gasification accelerator made of clay having a catalytic function and / or a heat medium function, the organic raw material is converted into a useful gas for gas / liquid fuel production, according to this technique. Under relatively mild temperature conditions of 400 ° C to 750 ° C, organic raw materials can be efficiently gasified without the formation of tar.

さらに特許文献２（特許第４５４９９１８号）に記載の方法においては、ガス化反応ゾーンと再生ゾーンとの隔壁として金属等の熱伝達性の高い材料を用いることによって、再生ゾーンからガス化反応ゾーンへの放射、伝導ならびに対流による熱伝達を行い、前記熱伝達がない場合と比べて再生ゾーンの温度を低減することができ、かつ装置の自動温度調整機能を高めることができる。 Further, in the method described in Patent Document 2 (Patent No. 4549918), by using a material having high heat conductivity such as metal as a partition wall between the gasification reaction zone and the regeneration zone, the regeneration zone is changed to the gasification reaction zone. By performing heat transfer by radiation, conduction, and convection, the temperature of the regeneration zone can be reduced as compared with the case where there is no heat transfer, and the automatic temperature adjustment function of the device can be enhanced.

本発明に係る固形物の回収技術は、上述したバイオマスのガス化技術に好適に適用され得るが、これらに限定されるものではなく、分離されるべき固形物が副生物として生成するバイオマスのガス化技術に広く適用され得る。 The solid matter recovery technique according to the present invention can be suitably applied to the above-mentioned biomass gasification technique, but is not limited thereto, and the solid matter to be separated is a biomass gas produced as a by-product. It can be widely applied to gasification technology.

本発明による固形物分離装置の模式的な平面図である。白抜きの矢印は流動層内の流動媒体と分離対象固形物の流れを示す。It is a schematic plan view of the solid matter separating apparatus by this invention. The white arrows indicate the flow of the fluidized medium and the solid matter to be separated in the fluidized bed. 本発明による固形物分離装置の流動層部分の模式的な立面図である。白抜きの矢印は流動層内の流動媒体の流れを示し、実線の矢印は、流動層に導入される以前のガス化剤の流れを示す。It is a schematic elevation view of the fluidized bed part of the solid matter separating apparatus by this invention. White arrows indicate the flow of the fluidized bed in the fluidized bed, and solid arrows indicate the flow of the gasifier before it was introduced into the fluidized bed. 本発明による固形物分離装置全体の模式的な側面図である。It is a schematic side view of the whole solid matter separating apparatus by this invention. 本発明の別の実施形態による固形物分離装置の模式的な平面図である。白抜きの矢印は流動層内の流動媒体と分離対象固形物の流れを示す。It is a schematic plan view of the solid matter separating apparatus according to another embodiment of this invention. The white arrows indicate the flow of the fluidized medium and the solid matter to be separated in the fluidized bed. 本発明の別の実施形態による固形物分離装置の流動層部分の模式的な立面図である。白抜きの矢印は流動層内の流動媒体の流れを示し、実線の矢印は、流動層に導入される以前のガス化剤の流れを示す。It is a schematic elevation view of the fluidized bed part of the solid matter separating apparatus by another embodiment of this invention. White arrows indicate the flow of the fluidized bed in the fluidized bed, and solid arrows indicate the flow of the gasifier before it was introduced into the fluidized bed. 本発明の別の実施形態による固形物分離装置全体の模式的な側面図である。It is a schematic side view of the whole solid matter separating apparatus by another embodiment of this invention.

以下、本発明を実施するための例示的な形態について、以下に添付の図面を用いて説明する。図面は単なる例示に過ぎず、本願発明の請求の範囲は、これらの形態ないし態様に限定されるものではない。 Hereinafter, exemplary embodiments for carrying out the present invention will be described with reference to the accompanying drawings. The drawings are merely examples, and the scope of claims of the present invention is not limited to these forms or embodiments.

本発明によれば、気泡流動層内に存在する固形物を、流動媒体から分別しつつ、流動層の外部に搬出し得る。具体例として、図１、２に示すように、ガス化反応ゾーン３と再生ゾーン２を備え、両者の間を触媒機能および/または熱媒体機能を有する粘土をガス化促進剤として気泡流動層を成す状態で循環させ、ガス化反応ゾーン３にバイオマス６を含む有機物を投入してガス化剤とガス化促進剤の存在下でガス化させ、炭素分などの吸着副生物が表面に沈着したガス化促進剤を再生ゾーン２に導いて、前記再生ゾーン２においてガス化促進剤に付着した吸着副生物を燃焼により、または部分燃焼と炭素質ガス化反応により除去し、このようにして再生された加熱状態のガス化促進剤を前記ガス化反応ゾーン３に再循環させる方式のバイオマスガス化装置1において、ガス化反応ゾーン３の気泡流動層の一部の濃厚相部上端付近に隣接させて、流動媒体の粒径よりは大きく、分離対象チャーの径よりは小さい多数の間隙を持つ捕捉帯を有し、水平に配置された、ベルト状のコンベア４と、そのコンベアにより移送された固形物を流動層外部に排出する排出装置から成る、チャー７の分離装置を設置する。 According to the present invention, the solid matter existing in the bubble fluidized bed can be carried out of the fluidized bed while being separated from the fluidized medium. As a specific example, as shown in FIGS. 1 and 2, a gasification reaction zone 3 and a regeneration zone 2 are provided, and a bubble flow layer is provided between the two using a gasification accelerator having a gasification function and / or a heat medium function. A gas in which an organic substance containing biomass 6 is put into the gasification reaction zone 3 and gasified in the presence of a gasifying agent and a gasification accelerator, and adsorption by-products such as carbon are deposited on the surface. The gasification accelerator was guided to the regeneration zone 2, and the adsorbed by-products adhering to the gasification accelerator in the regeneration zone 2 were removed by combustion or by partial combustion and carbonaceous gasification reaction, and thus regenerated. In the gasification apparatus 1 of the type in which the gasification accelerator in the heated state is recirculated to the gasification reaction zone 3, the gasification reaction zone 3 is adjacent to the upper end of a part of the bubble flow layer of the gasification reaction zone 3 and is adjacent to the upper end of the concentrated phase portion. A belt-shaped conveyor 4 having a large number of gaps having a large number of gaps larger than the particle size of the flow medium and smaller than the diameter of the char to be separated, and horizontally arranged, and the solid matter transferred by the conveyor. A char 7 separator is installed, which consists of a discharge device that discharges to the outside of the flow layer.

粘土をガス化促進剤とするバイオマスの流動層ガス化装置では、タールの吸着分解作用を持った粘土が、ガス化反応ゾーンに投入されたバイオマスを包囲するため、大径のバイオマス６を未粉砕で投入でき、粘土のせん断応力は小さいため、大径のバイオマスから生成するチャー７も大径である。したがって、上記のように設置されたコンベア4により、流動媒体とチャー７を、その径の違いにより分離することができる。 In a biomass fluidized bed gasifier that uses clay as a gasification accelerator, the large-diameter biomass 6 is uncrushed because the clay that has the adsorption and decomposition action of tar surrounds the biomass that has been put into the gasification reaction zone. Since the shear stress of the clay is small, the char 7 produced from the large-diameter biomass also has a large diameter. Therefore, the flow medium and the char 7 can be separated by the difference in diameter by the conveyor 4 installed as described above.

分離されたチャー７は、図３に示すように、コンベア４の連続的な運動により、流動層からの粒子の飛散を伴わない程度の位置まで水平に運ばれ、ついで、垂直方向に設置されたシュート１２により、落下し、ダブルダンパー１３等の外部との遮断機構を経て、外部に排出される。一方、流動層に近接した、粒子の飛散をともなう位置には、底板が流動層に向けて傾斜した緩衝ゾーン１０ａ、１０ｂを設けることによって、飛散した粒子を元の流動層に戻すことができる。 As shown in FIG. 3, the separated char 7 was horizontally carried to a position where particles were not scattered from the fluidized bed by the continuous motion of the conveyor 4, and then installed in the vertical direction. It falls by the chute 12 and is discharged to the outside through a blocking mechanism with the outside such as a double damper 13. On the other hand, the scattered particles can be returned to the original fluidized bed by providing the buffer zones 10a and 10b in which the bottom plate is inclined toward the fluidized bed at a position close to the fluidized bed and accompanied by the scattering of the particles.

本発明の好ましい一実施形態においては、ベルト状のコンベア４の下部の空塔速度を、隣接する流動層８の空塔速度よりも低くすることにより、図２に示されるようにベルト状のコンベア４に隣接する流動層８内に存在する固形物をベルト状のコンベア４の捕捉帯上に押し出す循環流を発生させることができる。このような循環流を発生させることにより、固形物がベルト状のコンベア４に捕獲される確率が高くなり、より効率的に固形物の分離を行うことができる。 In a preferred embodiment of the present invention, the belt-shaped conveyor 4 has a lower superficial velocity lower than that of the adjacent fluidized bed 8 so that the belt-shaped conveyor 4 has a belt-shaped conveyor as shown in FIG. It is possible to generate a circulating flow that pushes the solid matter existing in the fluidized bed 8 adjacent to 4 onto the trapping zone of the belt-shaped conveyor 4. By generating such a circulating flow, the probability that the solid matter is captured by the belt-shaped conveyor 4 increases, and the solid matter can be separated more efficiently.

本発明の別の好ましい実施形態において、例えば、ベルト状のコンベア４の下部の流動層の底板を、隣接する流動層8に向けて深くなるように傾斜させることによって、帯状搬送手段４に隣接する流動層８内に存在する固形物（チャー７）を帯状搬送手段４の捕捉帯上に押し出す循環流を、より発生させやすくすることができる。このように循環流をより効果的に発生させることにより、固形物７が帯状搬送手段４の捕捉面上に誘導される可能性が高くなり、より効率的に固形物の分離を行うことができる。 In another preferred embodiment of the present invention, for example, the bottom plate of the fluidized bed at the bottom of the belt-shaped conveyor 4 is inclined so as to be deeper toward the adjacent fluidized bed 8 so as to be adjacent to the strip-shaped transport means 4. It is possible to make it easier to generate a circulating flow that pushes the solid matter (char 7) existing in the fluidized bed 8 onto the trapping zone of the band-shaped conveyor 4. By generating the circulating flow more effectively in this way, the possibility that the solid matter 7 is guided on the trapping surface of the strip-shaped transport means 4 becomes high, and the solid matter can be separated more efficiently. ..

また、本発明の他の好ましい実施形態においては、帯状搬送手段４の駆動部を流動層８から隔離された位置に配置することができる。このように駆動部を流動層から離れた場所に配置することにより、駆動部が熱や湿気による影響を受けにくく、故障のリスクを低減させることができ装置自体の耐久性を向上させることができる点でも有利である。 Further, in another preferred embodiment of the present invention, the drive unit of the strip-shaped transport means 4 can be arranged at a position isolated from the fluidized bed 8. By arranging the drive unit at a location away from the fluidized bed in this way, the drive unit is less likely to be affected by heat and humidity, the risk of failure can be reduced, and the durability of the device itself can be improved. It is also advantageous in terms of points.

また、本発明の他の好ましい実施形態においては、図４〜６に示すように、帯状搬送手段４は、前記捕捉帯に代わり、固形物を分離・捕捉するためのコレクター１４を備えることができる。該コレクター１４は複数の刃を備え、該刃の間隔は、該固形物の径より小さく前記流動層の流動媒体をなす物質の径より大きい間隔である。該コレクター１４は、該帯状搬送手段に固形物を捕捉可能な態様で、複数個備えられることが好ましい。これにより、該帯状搬送手段が配置された位置の流動層付近に誘導された固形物を、該コレクターにより捕捉し、該帯状搬送手段と該コレクターの循環運動によって流動層から掻き上げ、ついで流動層装置外に連続的に分離・搬出することができる。 Further, in another preferred embodiment of the present invention, as shown in FIGS. 4 to 6, the band-shaped transport means 4 may include a collector 14 for separating / capturing solid matter in place of the trapping band. .. The collector 14 includes a plurality of blades, and the distance between the blades is smaller than the diameter of the solid material and larger than the diameter of the substance forming the fluidized medium of the fluidized bed. It is preferable that a plurality of collectors 14 are provided in the strip-shaped transport means in a manner capable of capturing solid matter. As a result, the solid matter induced near the fluidized bed at the position where the strip-shaped transport means is arranged is captured by the collector, and is scraped up from the fluidized bed by the circulating motion of the strip-shaped transport means and the collector, and then the fluidized bed. It can be continuously separated and carried out of the device.

また本発明の他の実施形態において、上述した実施形態の内の一部または全部を組み合わせることができる。 Further, in other embodiments of the present invention, some or all of the above-described embodiments can be combined.

本発明による固形物分離装置により固形物が分離される実施例について、以下、具体的に説明する。 Examples in which solid matter is separated by the solid matter separating apparatus according to the present invention will be specifically described below.

大径のチャーの生成例
長さ２．１ｍ、幅１．６ｍ、高さ３ｍの変形楕円形を隔壁で区切ったガス化反応ゾーン３と再生ゾーン２を備えたバイオマスガス化装置１において、スマトラ産アブラヤシ空房を４分の１に分割した、２０〜４５ｃｍのバイオマス６を原料にガス化を行った。投入する粘土触媒としては、平均粒径４５０μｍのインドネシア産粘土を用いた。主な運転条件は、空気比０．１、ガス化炉の温度６９０℃、スチーム／バイオマス比０．８２、バイオマス投入速度２５２ｋｇ（湿重量）／時である。この時、高位発熱量８．２９ＭＪ／Ｎｍ^３のガスが、１９６Ｎｍ^３／時得られ、冷ガス効率は４３．２％、生成ガス中のタール濃度は１３６ｍｇ／Ｎｍ^３であった。この時、投入したバイオマス中の炭素分の２０〜２５％の炭素分を含む、投入した空房片の外形を保ったチャー７が得られた。Example of generation of large-diameter chars Sumatra in a biomass gasification device 1 provided with a gasification reaction zone 3 and a regeneration zone 2 in which a deformed elliptical shape having a length of 2.1 m, a width of 1.6 m, and a height of 3 m is separated by a partition wall. Gasification was performed using 20 to 45 cm of biomass 6 as a raw material, which was obtained by dividing the produced oil palm air chamber into quarters. As the clay catalyst to be charged, Indonesian clay having an average particle size of 450 μm was used. The main operating conditions are an air ratio of 0.1, a gasifier temperature of 690 ° C., a steam / biomass ratio of 0.82, and a biomass input rate of 252 kg (wet weight) / hour. At this time, the gas of higher heating value 8.29MJ / Nm ³ is, 196 nm ³ / time obtained, the cold gas efficiency is 43.2%, the tar concentration in the product gas was 136 mg / Nm ^3. At this time, a char 7 containing 20 to 25% of the carbon content in the charged biomass and maintaining the outer shape of the charged air chamber piece was obtained.

流動媒体からの固形物の分離
（実施例１）
ガス化反応ゾーン３と再生ゾーン２が隔壁を隔てて存在する内部循環型気泡流動層コールドモデルの、ガス化反応ゾーン３に隣接して、図１、２および３に示すように固形物の分離・回収用のベルト状のコンベア(横方向２cm、縦方向３．５cmのひし形の間隙を多数有する捕捉帯を装備)を設置した。この装置に、平均粒子径２００μmの粘土粒子を充填し、流動層８をUo-Umf=０．１５m/s、ベルト状のコンベア下部を０．０６m/s(2Umf)の空塔速度になるように空気を導入して流動させた。そこに、直径３cm、長さ５〜１０cmの炭を導入して運転したところ、９割以上の炭が、ベルト状のコンベアにより系外に排出された。一方、炭を粉砕して、長径１cm以下の塊として投入したところ、排出される炭は見られなかった。Separation of solid matter from fluid medium (Example 1)
Separation of solids as shown in FIGS. 1, 2 and 3 adjacent to the gasification reaction zone 3 of the internal circulation type bubble fluidized bed cold model in which the gasification reaction zone 3 and the regeneration zone 2 are separated by a partition wall. -A belt-shaped conveyor for collection (equipped with a trapping band with many diamond-shaped gaps of 2 cm in the horizontal direction and 3.5 cm in the vertical direction) was installed. This device is filled with clay particles having an average particle diameter of 200 μm so that the fluidized bed 8 has a superficial velocity of Uo-Umf = 0.15 m / s and the lower part of the belt-shaped conveyor has a superficial velocity of 0.06 m / s (2 Umf). Air was introduced into the clay to make it flow. When charcoal with a diameter of 3 cm and a length of 5 to 10 cm was introduced there and operated, more than 90% of the charcoal was discharged to the outside of the system by a belt-shaped conveyor. On the other hand, when the charcoal was crushed and put in as a lump with a major axis of 1 cm or less, no discharged charcoal was observed.

（実施例２）
ガス化反応ゾーン３と再生ゾーン２が隔壁を隔てて存在する内部循環型気泡流動層コールドモデルの、ガス化反応ゾーン３に隣接して、図４、５および６に示すように固形物の分離・回収用のコレクター付チェーンコンベア４（コレクターの刃の間隔：１．５ｃｍ）を設置した。この装置に、平均粒子径３５０μｍの粘度粒子を充填し、流動層Uo-Umf=０．１０m/s、コンベア下部を０．１５m/s（１．５Umf）の空塔速度になるように空気を導入して流動させた。そこに、直径３cm、長さ５〜１０cmの炭を導入して運転したところ、９割以上の炭が、コンベアにより系外に排出された。一方、炭を粉砕して、長径１cm以下の塊として投入したところ、排出される炭は見られなかった。(Example 2)
Separation of solids as shown in FIGS. 4, 5 and 6 adjacent to the gasification reaction zone 3 of the internal circulation type bubble fluidized bed cold model in which the gasification reaction zone 3 and the regeneration zone 2 are separated by a partition wall. -A chain conveyor 4 with a collector for collection (interval between collector blades: 1.5 cm) was installed. This device is filled with viscous particles having an average particle diameter of 350 μm, and air is introduced so that the fluidized bed Uo-Umf = 0.10 m / s and the lower part of the conveyor have a superficial velocity of 0.15 m / s (1.5 Umf). Introduced and fluidized. When charcoal with a diameter of 3 cm and a length of 5 to 10 cm was introduced and operated there, more than 90% of the charcoal was discharged to the outside of the system by a conveyor. On the other hand, when the charcoal was crushed and put in as a lump with a major axis of 1 cm or less, no discharged charcoal was observed.

１バイオマスガス化装置
２再生ゾーン
３ガス化反応ゾーン
４ベルト状のコンベア
５流動媒体
６バイオマス
７チャー
８流動層
９ガス化剤
１０ａ緩衝ゾーン
１０ｂ緩衝ゾーン
１１駆動部
１２シュート
１３ダブルダンパー
１４コレクター1 Biomass gasifier 2 Regeneration zone 3 Gasification reaction zone 4 Belt-shaped conveyor 5 Fluid medium 6 Biomass 7 Char 8 Fluidized bed 9 Gasifier 10a Buffer zone 10b Buffer zone 11 Drive unit 12 Shoot 13 Double damper 14 Collector

Claims

A device for separating relatively coarse solids existing in a fluidized bed from a fluidized bed and continuously carrying them out of the fluidized bed device.
A trapping zone having a large number of gaps smaller than the diameter of the solid material and larger than the diameter of the substance forming the fluidized bed of the fluidized bed, and having a diameter that allows the fluidized medium to pass through and selectively traps the solid material. With a strip-shaped transport means
It has a power means for introducing a part of the strip-shaped transport means into the fluidized bed device and continuously circulating the strip-shaped transport means.
The solid matter selectively captured by the strip-shaped transport means is continuously separated and carried out of the fluidized bed device so as to be carried out.
An apparatus , characterized in that the strip-shaped transport means is provided so as to move horizontally in the vicinity of the upper end of a concentrated phase portion of the fluidized bed for a certain section.

The strip-shaped transport means includes a collector that separates and traps solid matter in place of the trapping zone, and the distance between the blades of the collector is smaller than the diameter of the solid matter and smaller than the diameter of the substance forming the fluidized medium of the fluidized bed. The large device of claim 1.

The device according to claim 2 , wherein the fluidized bed is a bubble fluidized bed.

The device according to any one of claims 1 to 3 , wherein the strip-shaped transport means comprises a chain conveyor.

In the fluidized bed, a device for making a difference between the superficial velocity of the fluidized bed at the position where the strip-shaped transport means is arranged and the superficial velocity of the other fluidized bed portion is further provided, and the solid matter is transported in the strip-shaped transport. The device according to any one of claims 1 to 4 , wherein the device is guided on a catching surface of the means.

The apparatus according to any one of claims 1 to 5 , which is introduced into a fluidized bed gasification apparatus for biomass.

The device according to claim 6 , wherein the solid substance to be separated is a char derived from biomass.