JPS587339B2 - KiyuuchiyakusaretakiyuuchiyakuzainonetsuTexaiseinotamenokariyusouhannouro - Google Patents
KiyuuchiyakusaretakiyuuchiyakuzainonetsuTexaiseinotamenokariyusouhannouroInfo
- Publication number
- JPS587339B2 JPS587339B2 JP50130581A JP13058175A JPS587339B2 JP S587339 B2 JPS587339 B2 JP S587339B2 JP 50130581 A JP50130581 A JP 50130581A JP 13058175 A JP13058175 A JP 13058175A JP S587339 B2 JPS587339 B2 JP S587339B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- adsorbent
- regeneration
- fluidized
- activated carbon
- 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.)
- Expired
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/36—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed through which there is an essentially horizontal flow of particles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3416—Regenerating or reactivating of sorbents or filter aids comprising free carbon, e.g. activated carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2220/00—Aspects relating to sorbent materials
- B01J2220/50—Aspects relating to the use of sorbent or filter aid materials
- B01J2220/66—Other type of housings or containers not covered by B01J2220/58 - B01J2220/64
Description
【発明の詳細な説明】
本発明は、吸着方法特に汚染された吸着剤を再生する方
法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to adsorption methods, particularly methods for regenerating contaminated adsorbents.
本発明は特に、特性及び／又は粒度の異なる汚染された
粒状吸着剤、とりわけ廃水成分で汚染又は飽和された吸
着剤、の流動状態における同時的熱再生に関する。The invention particularly relates to the simultaneous thermal regeneration in the fluid state of contaminated particulate adsorbents of different properties and/or particle sizes, especially adsorbents contaminated or saturated with wastewater components.
有機物質は例えば活性炭、酸化アルミニウム、シリカゲ
ルの如き吸着剤により廃水から除去される。Organic substances are removed from wastewater by adsorbents such as activated carbon, aluminum oxide, and silica gel.
一般に、廃水は単一タイプの物質或は単一種類の物質の
みを含んでいるのではなく、むしろ多くの物質の複雑な
混合物を含んでいる。In general, wastewater does not contain a single type of substance or only a single type of substance, but rather a complex mixture of many substances.
この結果単一の吸着剤では廃水から有機物質を吸着する
ことが不充分であることが判明している。As a result, it has been found that a single adsorbent is insufficient to adsorb organic substances from wastewater.
一方においては、一つ以上の吸着剤例えば極性および非
極性表面を有する酸化アルミニウムと活性炭を用いて高
度の浄化が可能である。On the one hand, a high degree of purification is possible using one or more adsorbents such as aluminum oxide and activated carbon with polar and non-polar surfaces.
更に別のやり方は直列に配置された複数の浄化段を設け
、その各段において粒度の異なる同一の吸着剤、例えば
活性炭を使用することである。Yet another option is to provide several purification stages arranged in series, each using the same adsorbent with a different particle size, such as activated carbon.
汚染された吸着剤の熱再生は従来主として多段式炉又は
回転管状炉内で行われてきた。Thermal regeneration of contaminated adsorbents has traditionally been carried out primarily in multi-stage furnaces or rotary tube furnaces.
この場合吸着剤は再生炉内を連続的に通過する。In this case, the adsorbent passes continuously through the regeneration furnace.
再生炉は吸着剤を静かに処理し得るのみでなく、良好な
熱及び材料移動特性が得られ且つ滞留時間が短かいよう
に設計されねばならない。The regeneration furnace must not only be able to process the adsorbent quietly, but must also be designed to provide good heat and material transfer properties and short residence times.
多段式炉又は回転管状炉によって達成され得る熱及び材
料移動特性の実質的向上は、流動層反応装置又は炉を用
いることによって可能にされる。The substantial improvements in heat and material transfer properties that can be achieved with multistage furnaces or rotary tube furnaces are made possible by using fluidized bed reactors or furnaces.
かくて、例えば活性炭の如き吸着剤の再生を、上下関係
に配置した複数個の個々の流動層を有する流動層反応装
置の中で実施することが周知となってきた。It has thus become well known to carry out the regeneration of adsorbents, such as activated carbon, in fluidized bed reactors having a plurality of individual fluidized beds arranged one above the other.
この場合流動化ガス並びに気化又はガス化剤は再生され
るべき吸着剤に対して向流関係に通される。In this case, the fluidizing gas as well as the vaporizing or gasifying agent are passed in countercurrent relation to the adsorbent to be regenerated.
吸着剤は多段流動層反応装置を頂部から底部へと連続し
て通過する。The adsorbent passes continuously through the multistage fluidized bed reactor from top to bottom.
この多段流動層反応装置は上述の利点即ち向上された熱
及び材料移動特性を有するが、それにもかゝわらず幾つ
かのむしろ重大な欠点を同時に有している。Although this multistage fluidized bed reactor has the advantages mentioned above, namely improved heat and material transfer properties, it nevertheless simultaneously has some rather significant disadvantages.
例えば、比較的大きい反応装置容積を必要とする。For example, a relatively large reactor volume is required.
更に、個々の段は相互にパイプで連結され、吸着剤は１
つの段の溢れ堰を通り越した後これらのパイプを通って
次の下方段に下向きに移動しなければならない（ドイツ
国特許第９５１，８６４号）。Furthermore, the individual stages are interconnected with pipes, and the adsorbent is
After passing over one stage of overflow weir, it has to move downward through these pipes to the next lower stage (German Patent No. 951,864).
更に、流動化ガスが通過する有孔壁を備えた細長い長方
形の流動層反応装置が周知である。Furthermore, elongated rectangular fluidized bed reactors with perforated walls through which fluidizing gas passes are well known.
この場合、垂直に配置され流動抑制作用をする邪魔板が
有孔壁の上方に設けられており、処理されている固体粒
子の移動方向に対し横方向に延在している。In this case, a vertically disposed flow-suppressing baffle is provided above the perforated wall and extends transversely to the direction of movement of the solid particles being treated.
流動抑制はこの垂直に配置された邪魔板に設けられた開
口により行われる。Flow suppression is achieved through openings provided in this vertically disposed baffle.
この構造は、例えば、赤熱温度での水蒸気又は活性化ガ
スによる炭素質物質の活性化の如き操作中に個々の固体
粒子を均一に処理することを意図している（ドイツ国特
許第９７１，４１７号）。This structure is intended for the uniform treatment of individual solid particles during operations such as the activation of carbonaceous materials with steam or activated gases at red-hot temperatures (German Patent No. 971,417). issue).
然しこの型式の構造は、活性炭粒子の一部が活性化され
過ぎて活性炭の損失を生ずるので、実際上活性炭の再生
に対しては不適当であることが判明している。However, this type of structure has been found to be unsuitable in practice for the regeneration of activated carbon, since some of the activated carbon particles become too activated, resulting in a loss of activated carbon.
本発明の目的は、吸着剤の再生に対する改善された方法
を提供することである。It is an object of the present invention to provide an improved method for regeneration of adsorbents.
本発明の別の目的は、直列に配置された浄化段内に収容
されている特性及び／又は粒度の異なる吸着剤によって
作動する吸着処理用流動層反応装置内での粒状吸着剤の
再生における実質的単純化に対する手段を講ずることで
ある。Another object of the present invention is to provide effective regeneration of granular adsorbents in fluidized bed reactors for adsorption processes operated by adsorbents of different properties and/or particle sizes housed in purification stages arranged in series. It is important to take steps to simplify the process.
上記の目的並びに説明が進むにつれて明瞭となる他の目
的は、本発明により達成される。The above objects, as well as other objects that will become apparent as the description progresses, are achieved by the present invention.
本発明の一面は、汚染された粒状吸着剤の流動状態にお
ける熱再生に対する装置即ち流動層反応装置に関する。One aspect of the present invention relates to an apparatus for thermal regeneration of contaminated particulate adsorbent in a fluidized state, ie, a fluidized bed reactor.
この流動層反応装置は、吸着剤を再生するように汚染さ
れた粒状吸着剤を流動状態で熱処理するための別々の第
１及び第２帯域を有する再生室を含含する。The fluidized bed reactor includes a regeneration chamber having separate first and second zones for heat treating contaminated particulate adsorbent in a fluidized state to regenerate the adsorbent.
入口装置が汚染された吸着剤を上記帯域に導入するため
設けられている。An inlet device is provided for introducing contaminated adsorbent into the zone.
出口装置が再生された吸着剤を上記帯域から取出すため
設けられている。An outlet device is provided for removing regenerated adsorbent from the zone.
上記流動層反応装置は更に、汚染された吸着剤を流動化
して熱処理するための装置を含み、この流動化して熱処
理する装置は高温の流動化ガスを第１及び第２帯域の両
方に供給するように構成された燃焼室を含んでいる。The fluidized bed reactor further includes an apparatus for fluidizing and heat treating the contaminated adsorbent, the fluidizing and heat treating apparatus supplying a hot fluidizing gas to both the first and second zones. It includes a combustion chamber configured as follows.
ガス出口が第１及び第２帯域の両方から流動化ガスを排
出するため再生室内に設けられている。A gas outlet is provided within the regeneration chamber for discharging fluidizing gas from both the first and second zones.
本発明の有利な１実施例によれば、入口装置は汚染され
た吸着剤を第１処理帯域に導入するための第１入口と、
第２処理帯域に汚染された吸着剤を導入するための実質
的に独立した別個の第２入口とを含んでいる。According to an advantageous embodiment of the invention, the inlet device comprises a first inlet for introducing contaminated adsorbent into the first treatment zone;
and a substantially separate and separate second inlet for introducing contaminated adsorbent into the second treatment zone.
本発明の更に好適な実施例においては、出口装置は再生
された吸着剤を第１処理帯域から取出すための第１出口
と、第２処理帯域から再生された吸着剤を取出すための
実質的に独立した別個の第２出口とを含んでいる。In a further preferred embodiment of the invention, the outlet device includes a first outlet for removing regenerated adsorbent from the first treatment zone and a substantially elongated outlet for removing regenerated adsorbent from the second treatment zone. an independent and separate second outlet.
本発明の他の一面は、汚染された粒状吸着剤を再生する
方法に関する。Another aspect of the invention relates to a method of regenerating contaminated particulate adsorbent.
この方法は、汚染された粒状吸着剤の第１の量を第１再
生帯域内に導入すること、及び第１再生帯域と共通の部
屋内に配置された別個の第２再生帯域内に汚染された吸
着剤の第２の量を導入することを包含する。The method includes introducing a first amount of contaminated particulate adsorbent into a first regeneration zone and a second, separate regeneration zone disposed in a common chamber with the first regeneration zone. and introducing a second amount of adsorbent.
吸着剤の第１及び第２の量は、共通の燃焼帯域から高温
ガスを第１及び第２再生帯域に供給することにより流動
化されて再生される。The first and second quantities of adsorbent are fluidized and regenerated by supplying hot gas from a common combustion zone to the first and second regeneration zones.
再生された吸着剤の第１及び第２の量は第１及び第２再
生帯域から引出され、流動化して再生するガスは共通の
排出口を通って第１及び第２再生帯域から排出される。First and second quantities of regenerated adsorbent are withdrawn from the first and second regeneration zones, and fluidized regeneration gas is discharged from the first and second regeneration zones through a common outlet. .
本発明の方法の好適実施例によれば、第１再生帯域内へ
の吸着剤の第１の量の導入は第２再生帯域内への吸着剤
の第２の量の導入とは別個に且つ実質的に独立して行わ
れる。According to a preferred embodiment of the method of the invention, the introduction of the first amount of adsorbent into the first regeneration zone is separate from and separate from the introduction of the second amount of adsorbent into the second regeneration zone. performed virtually independently.
本発明の方法の別の好適実施例は、第１再生帯域からの
再生された吸着剤の第１の量の引出しを、第２再生帯域
からの再生された吸着剤の引出しとは別個に且つ実質的
に独立して行うことを意図している。Another preferred embodiment of the method of the invention provides for the withdrawal of the first quantity of regenerated adsorbent from the first regeneration zone to be separate from the withdrawal of regenerated adsorbent from the second regeneration zone and It is intended to be substantially independent.
本発明の特徴と思考される新規な特徴は特許請求の範囲
に記載されている。The novel features that are considered characteristic of the invention are set forth in the claims.
然し、本発明自体はその構成及び作動方法について附加
的目的および利点と共に、代表的実施例に関する以下の
説明を添付図面を参照して読めば良く理解されるであろ
う。The invention itself, however, as well as its construction and method of operation, together with additional objects and advantages, will be better understood from the following description of representative embodiments, taken in conjunction with the accompanying drawings.
本発明は、特性及び／又は粒度の異なる粒状吸着剤、特
に廃水成分で汚染又は飽和された吸着剤の流動状態にお
ける同時的熱再生に関する。The present invention relates to simultaneous thermal regeneration in the fluid state of particulate adsorbents of different properties and/or particle sizes, especially adsorbents contaminated or saturated with wastewater components.
本発明の好適実施例は、気化又はガス化剤を含有してい
る流動化ガスを使用して個々の流動層内の吸着剤を加熱
して熱再生を行うことを意図している。A preferred embodiment of the present invention contemplates the use of a fluidizing gas containing a vaporizing or gasifying agent to heat the adsorbent within the individual fluidized beds for thermal regeneration.
空気又は酸素もまた適当又は好適と思われる場合には流
動層に供給され得る。Air or oxygen may also be supplied to the fluidized bed if deemed appropriate or preferred.
熱再生は、断面が実質的に長方形又は正方形であり長さ
対幅の比が約２より大きい細長い流動層反応装置内で行
われるのが好ましい。Thermal regeneration is preferably carried out in an elongated fluidized bed reactor having a substantially rectangular or square cross-section and a length-to-width ratio greater than about 2.
流動層反応装置には邪魔板が設けられ、これら邪魔板は
１つ又は１つ以上の流動層の内部に配置され且つ再生さ
れている吸着剤粒子の移動方向に対し横方向に延在して
吸着剤の流動を抑制するようになっている。The fluidized bed reactor is provided with baffles which are disposed within the one or more fluidized beds and which extend transversely to the direction of movement of the adsorbent particles being regenerated. It is designed to suppress the flow of adsorbent.
邪魔板は垂直方向に位置調節可能であり且つ流動層上面
から流動層内に浸漬されるように配置される。The baffle plate is vertically adjustable in position and is arranged so as to be immersed into the fluidized bed from the top surface of the fluidized bed.
本発明の目的は、共通の流動層反応装置内に流動層を相
互に分離して配置することにより達成される。The object of the invention is achieved by arranging the fluidized beds separated from each other within a common fluidized bed reactor.
流動層は横に並べて又は上下に配置される。各流動層に
は吸着剤導入のための自動的且つ独立した入口装置並び
に再生された吸着剤取出しのための自動的且つ独立した
出口装置が設けられている。The fluidized beds are arranged side by side or one above the other. Each fluidized bed is provided with an automatic and independent inlet device for introducing the adsorbent and an automatic and independent outlet device for removing the regenerated adsorbent.
一方、流動化ガス発生のための共通の燃焼室が設けられ
更に流動層からの廃ガスのための共通の排出装置が設け
られている。On the one hand, a common combustion chamber is provided for the generation of fluidizing gas and also a common discharge device for the waste gas from the fluidized bed.
１つ又は１つ以上の有孔壁が燃焼室と流動層が形成され
る帯域との間に設けられ、流動化ガスが燃焼室から流動
層帯域へ移動し得るようになっている。One or more perforated walls are provided between the combustion chamber and the zone in which the fluidized bed is formed to allow fluidizing gas to pass from the combustion chamber to the fluidized bed zone.
流動層が上下に配置されている場合には各流動層の下方
にそれぞれ有孔壁が設けられる。When the fluidized beds are arranged one above the other, a perforated wall is provided below each fluidized bed.
一方、流動層が横に並べて配置されている場合には単一
の有孔壁が燃焼室と流動層との間に設けられる。On the other hand, if the fluidized beds are arranged side by side, a single perforated wall is provided between the combustion chamber and the fluidized bed.
上述の如く、流動層はそれぞれの下方に有孔壁を備えて
相互上下関係に配置することができる。As mentioned above, the fluidized beds can be arranged one above the other with perforated walls below each.
一方は熱を吸収してより高い温度で再生される吸着剤（
例えば、水蒸気による活性炭の再生）であり、他方は熱
を遊離してより低い温度で再生される吸着剤（例えば、
空気による酸化アルミニウムの再生）である２つの異な
る吸着剤が再生されるべき場合には、より高温度で起る
再生を２つの流動層の下方の流動層で実施し、より低温
度で起る再生を上方の流動層で実施するのが有利である
。One is an adsorbent that absorbs heat and is regenerated at higher temperatures (
one is an adsorbent that liberates heat and is regenerated at a lower temperature (e.g. activated carbon regeneration with steam); the other is an adsorbent that liberates heat and is regenerated at a lower temperature
If two different adsorbents are to be regenerated (regeneration of aluminum oxide with air), the regeneration that occurs at the higher temperature is carried out in the lower fluidized bed of the two fluidized beds, and the regeneration that occurs at the lower temperature Preferably, the regeneration is carried out in an upper fluidized bed.
この場合、必要とされる酸素を空気又は実質上純酸素の
形態で上方流動層用の有孔壁即ち上方有孔壁の直下に導
入すると更に有利であることが判った。In this case, it has been found to be further advantageous to introduce the required oxygen in the form of air or essentially pure oxygen into the perforated wall for the upper fluidized bed, i.e. directly below the upper perforated wall.
単一種類の吸着剤のみを使用するのであるがその吸着剤
の粒度が異なる場合には、横に並べて配置された流動層
を使用するのが好適である。If only a single type of adsorbent is used, but the particle size of the adsorbent is different, it is preferred to use fluidized beds arranged side by side.
かくて本発明によれば燃焼室上方に位置する有孔壁を、
吸着剤の入口から出口まで延在する垂直壁により、２つ
の独立した部分に分割することができる。Thus, according to the present invention, the perforated wall located above the combustion chamber is
A vertical wall extending from the inlet to the outlet of the adsorbent allows it to be divided into two separate parts.
換言すれば燃焼室上方に設けた有孔壁上方で吸着剤入口
から出口まで延在する垂直壁を設けて流動層に対す２つ
の分離したチャンネルを形成することができる。In other words, above the perforated wall above the combustion chamber, a vertical wall can be provided extending from the adsorbent inlet to the outlet to form two separate channels for the fluidized bed.
個々の流動層を流過した後の流動化ガス、即ちより正確
に云えば、流動化ガスの反応によって生じたガスは集め
られて後処理を受ける、即ち異なる流動層からの流動化
ガスは一緒になって後処理を受ける。The fluidizing gas after passing through the individual fluidized beds, or more precisely the gas produced by the reaction of the fluidizing gases, is collected and subjected to after-treatment, i.e. the fluidizing gases from different fluidized beds are combined and undergo post-processing.
本発明による流動層反応装置の特別の利点は、異なる吸
着剤即ち特性及び／又は粒度の異なる吸着剤の再生が異
なる流動層に対し共通の流動化ガス発生用燃焼室に組合
わされて行われることと、流動化ガスの廃ガスが一緒に
後処理されることとにある。A particular advantage of the fluidized bed reactor according to the invention is that the regeneration of different adsorbents, i.e. adsorbents with different properties and/or particle sizes, is carried out for different fluidized beds in combination in a common combustion chamber for generation of fluidizing gas. and that the waste gas of the fluidizing gas is also after-treated.
このようにして、吸着剤の再生は別々の流動層反応装置
より容積の小さいコンパクトな装置内で行われ得、更に
再生は別々の流動層反応装置で行われる再生とは反対に
エネルギー損失が実質的に減少される状態で行われ得る
。In this way, regeneration of the adsorbent can be carried out in a compact device with a smaller volume than a separate fluidized bed reactor, and furthermore, the regeneration involves virtually no energy loss, as opposed to regeneration carried out in a separate fluidized bed reactor. It can be carried out in a state where the amount of water is reduced.
本発明による流動層反応装置及びその作動が図面を参照
して以下に記述される。The fluidized bed reactor according to the invention and its operation will be described below with reference to the drawings.
第１図及び第２図に示す実施例においては、再生される
べき湿った吸着剤は入口装置５を介して流動層１内に導
入される。In the embodiment shown in FIGS. 1 and 2, the wet adsorbent to be regenerated is introduced into the fluidized bed 1 via an inlet device 5. In the embodiment shown in FIGS.
流動層は幅Ｂ１、長さＬを有する。The fluidized bed has a width B1 and a length L.
流動層１内に導入された吸着剤はこの場合活性炭とする
。The adsorbent introduced into the fluidized bed 1 is in this case activated carbon.
活性炭は流動層内を流過した後、垂直方向に調節可能の
堰６を通過して再生された状態で流動層から排出される
。After flowing through the fluidized bed, the activated carbon passes through a vertically adjustable weir 6 and is discharged from the fluidized bed in a regenerated state.
流動層１内に延在する３つの邪魔板２，３，４は流動層
の長さＬに沿い間隔を置いて配置され入口装置５から堰
６に至る活性炭の真直ぐな流動を妨げる。Three baffles 2, 3, 4 extending within the fluidized bed 1 are spaced apart along the length L of the fluidized bed and prevent straight flow of activated carbon from the inlet device 5 to the weir 6.
邪魔板２，３，４は距離ｌだけ相互離隔しており、流動
層１内へ浸漬される深さは堰６に向う方向において増加
する。The baffles 2, 3, 4 are separated from each other by a distance l, the depth of immersion into the fluidized bed 1 increasing in the direction towards the weir 6.
即ち邪魔板２の浸漬深さは最も浅く邪魔板４は最も深く
浸漬している。That is, the immersion depth of the baffle plate 2 is the shallowest, and the immersion depth of the baffle plate 4 is the deepest.
邪魔板２，３，４は垂直方向に変位し得るように装架さ
れている。The baffle plates 2, 3, 4 are mounted so as to be vertically displaceable.
再生された活性炭は容器１６内に送り込まれて容器内で
水冷却され、活性炭は水力で吸着反応炉に移送される。The regenerated activated carbon is fed into the container 16, where it is cooled with water, and the activated carbon is transferred to the adsorption reactor by hydraulic power.
流動層１は下方流動層を形成し、その上方に別の流動層
７が設けられている。The fluidized bed 1 forms a lower fluidized bed, above which another fluidized bed 7 is provided.
再生されるべき湿った吸着剤は入口装置８を介して流動
層７内に導入される。The wet adsorbent to be regenerated is introduced into the fluidized bed 7 via an inlet device 8 .
流動層７は幅Ｂ２、長さＬを有する。The fluidized bed 7 has a width B2 and a length L.
流動層７内に導入された吸着剤はこの場合酸化アルミニ
ウムの如き無機吸着剤とする。The adsorbent introduced into the fluidized bed 7 is in this case an inorganic adsorbent such as aluminum oxide.
無機吸着剤は流動層７を流過した後、垂直方向に調節可
能の堰１２を通過して再生された状態で流動層から排出
される。After flowing through the fluidized bed 7, the inorganic adsorbent passes through a vertically adjustable weir 12 and is discharged from the fluidized bed in a regenerated state.
３つの邪魔板９，１０．１１は流動層７内に延在し且つ
流動層の長さＬに沿い間隔を置いて配置されている。Three baffles 9, 10, 11 extend within the fluidized bed 7 and are spaced apart along the length L of the fluidized bed.
この場合邪魔板９，１０，１１は距離ｌだけ相互離隔し
ており、邪魔板９，１０，１１が流動層７内へ浸漬する
深さは堰１２に向う方向において増加し、且つ邪魔板９
，１０，１１は垂直方向に変位され得るように装架され
ている。In this case, the baffles 9, 10, 11 are separated from each other by a distance l, the depth of immersion of the baffles 9, 10, 11 into the fluidized bed 7 increases in the direction towards the weir 12, and
, 10, 11 are mounted such that they can be displaced vertically.
再生された無機吸着剤は流動層７から容器１５内に送り
込まれて容器内で水冷却される。The regenerated inorganic adsorbent is sent from the fluidized bed 7 into the container 15 and cooled with water within the container.
無機吸着剤は水力で容器１５から吸着反応炉に移送され
る。The inorganic adsorbent is hydraulically transferred from the vessel 15 to the adsorption reactor.
有孔壁１８が流動層１の下方に配置され、有孔壁１９が
流動層γの下方に配置されている。A perforated wall 18 is arranged below the fluidized bed 1, and a perforated wall 19 is arranged below the fluidized bed γ.
２つの流動層１，７に対し必要とされる流動化ガスは燃
焼室１３内にて発生され、有孔壁１８，１９を経て流動
層１，７内に上昇する。The fluidizing gas required for the two fluidized beds 1, 7 is generated in the combustion chamber 13 and rises into the fluidized beds 1, 7 via perforated walls 18, 19.
有孔壁１８，１９を経て流動層１，７を形成し維持する
ために必要な流動化ガスは燃焼室１３内にて、水を加え
ながら化学量論的燃焼により発生される。The fluidizing gas required to form and maintain the fluidized beds 1, 7 via the perforated walls 18, 19 is generated in the combustion chamber 13 by stoichiometric combustion with the addition of water.
両方の流動層１．７からの流動化ガス廃気は同一の排気
筒１７を通して流動層反応装置から排出される。The fluidizing gas waste gas from both fluidized beds 1.7 is discharged from the fluidized bed reactor through the same stack 17.
このようにして排出された流動化ガスは好ましからぬ成
分を含まないように洗滌操作を受ける。The fluidizing gas discharged in this way is subjected to a cleaning operation so that it is free of undesirable components.
流動層７内にて無機吸着剤の再生に要する空気は導管１
４を介して上方有孔壁１９の下方で流動層反応装置内に
導入される。The air required for regenerating the inorganic adsorbent in the fluidized bed 7 is supplied to the conduit 1.
4 into the fluidized bed reactor below the upper perforated wall 19.
本発明による二層式流動層反応装置の作動が実施例につ
いて説明されるが、これは本発明を何等限定するもので
はない。The operation of a two-layer fluidized bed reactor according to the invention will be described by way of example, which is not intended to limit the invention in any way.
例１ 毎時１８０立方米のセルローズ廃水が浄化される。Example 1 180 cubic meters of cellulose wastewater is purified every hour.
廃水は４５０ｇｒ／ｍ３のＴＯＣ含有量を有する。ＴＯ
Ｃは全有機炭素を意味する。The wastewater has a TOC content of 450 gr/m3. T.O.
C means total organic carbon.
廃水の浄化に対して２つの別々の直列に配置された吸着
器が使用され、それぞれ粒度１．５〜２．５ｍｍの酸化
アルミニウム４００ｋｇ／ｈと粒度１．５ 〜２ｍｍの
活性炭２００ｋｇ／ｈとを必要とする。Two separate adsorbers arranged in series were used for the purification of wastewater, each containing 400 kg/h of aluminum oxide with a particle size of 1.5-2.5 mm and 200 kg/h of activated carbon with a particle size of 1.5-2 mm. I need.
活性炭の再生は長さ３． ２ｍ、幅０．８ｍを有する流
動層内にて行われる。The length of activated carbon regeneration is 3. It is carried out in a fluidized bed with a width of 2 m and a width of 0.8 m.
３つの邪魔板は流動層内に相互０．８ｍの間隔を置いて
配置される。Three baffles are placed in the fluidized bed with a distance of 0.8 m from each other.
これら邪魔板は、活性炭入口から出口への方向において
考えたとき邪魔下の自由通路は、流動化された活性炭の
層の高さのそれぞれ６０％、５０％、４０％に等しくな
るように配置される。These baffles are arranged so that the free passage under the baffle is equal to 60%, 50%, and 40% of the height of the bed of fluidized activated carbon, respectively, when considered in the direction from the activated carbon inlet to the outlet. Ru.
酸化アルミニウムの再生は前述の活性炭に対する流動層
の上方に配置された流動層内にて行われる。The regeneration of the aluminum oxide takes place in a fluidized bed placed above the fluidized bed for the activated carbon described above.
酸化アルミニウム流動層は長さ３．２ｍ、幅０．４ｍを
有する。The aluminum oxide fluidized bed has a length of 3.2 m and a width of 0.4 m.
活性炭流動層と同様に３つの邪魔板が酸化アルミニウム
流動層内に配置されている。Similar to the activated carbon fluidized bed, three baffles are arranged within the aluminum oxide fluidized bed.
酸化アルミニウム流動層内の邪魔板は活性炭流動層にお
ける邪魔板と同じ深さに浸漬されている。The baffles in the aluminum oxide fluidized bed are immersed to the same depth as the baffles in the activated carbon fluidized bed.
酸素を含まず且つ容積比で５５％の水蒸気を含む反応ガ
スの２４００ｍ３／ｈが燃焼室内にて発生され流動化ガ
スとして利用される。2400 m3/h of reaction gas containing no oxygen and containing 55% water vapor by volume is generated in the combustion chamber and used as fluidizing gas.
下方の有孔壁即ち活性炭流動層下方の有孔壁より下方の
温度は１１００℃である。The temperature below the perforated wall below the activated carbon fluidized bed is 1100°C.
流動化ガスは第１流動層即ち活性炭流動層を温度８００
℃にて去り、１３００ｍ３／ｈの空気の附加により温度
６００℃に冷却される。The fluidizing gas moves the first fluidized bed, that is, the activated carbon fluidized bed, to a temperature of 800°C.
℃ and is cooled to a temperature of 600 ℃ by adding 1300 m3/h of air.
次いで流動化ガスは上方の流動層即ち酸化アルミニウム
流動層を何等の温度変化を受けることなく流過する。The fluidizing gas then flows through the upper fluidized bed, ie the aluminum oxide fluidized bed, without undergoing any temperature change.
次いで流動化ガス廃気は冷却され且つ洗滌操作によりＨ
ＣｌおよびＳＯ２が取除かれる。The fluidizing gas waste gas is then cooled and H
Cl and SO2 are removed.
第３図及び第４図に示す実施例は幅Ｂ１、長さＬを有す
る流動層２４と、長さＬ、幅Ｂ１より小さい幅Ｂ２を有
する流動層２３を含む。The embodiment shown in FIGS. 3 and 4 includes a fluidized bed 24 having a width B1 and a length L, and a fluidized bed 23 having a length L and a width B2 smaller than the width B1.
流動層２３，２４は横に並べて配置され且つ隔壁２０に
より相互分離されている。The fluidized beds 23 and 24 are arranged side by side and separated from each other by a partition wall 20.
幅広の流動層２４内にて再生されるべき湿った吸着剤は
入口装置２２を介して流動層２４内に導入される。The wet adsorbent to be regenerated in the wide fluidized bed 24 is introduced into the fluidized bed 24 via the inlet device 22 .
流動層２４内に導入された吸着剤は比較的に粗い粒度を
有する活性炭とする。The adsorbent introduced into the fluidized bed 24 is activated carbon having a relatively coarse particle size.
流動層２４を通過した後、活性炭は垂直方向に調節可能
の堰２８を通過し再生された状態で流動層２４から排出
される。After passing through the fluidized bed 24, the activated carbon passes through a vertically adjustable weir 28 and is discharged from the fluidized bed 24 in a regenerated state.
流動層２４内に延在する３らの邪魔板２５，２６，２７
は流動層の長さＬに沿って配置され入口装置２２から流
動層２４を通って堰２８に至る活性炭の真直ぐな流動を
抑制する。Three baffle plates 25, 26, 27 extending within the fluidized bed 24
are arranged along the length L of the fluidized bed to inhibit straight flow of activated carbon from the inlet device 22 through the fluidized bed 24 to the weir 28.
邪魔板２５，２６，２７は距離ｌだけ相互に分離されて
いる。The baffles 25, 26, 27 are separated from each other by a distance l.
邪魔板２５，２６，２７は垂直方向に変位し得るように
装架される。The baffle plates 25, 26, 27 are mounted so as to be vertically displaceable.
流動層２４から再生された活性炭は容器３０内に導かれ
て容器内で水により冷却される。The activated carbon regenerated from the fluidized bed 24 is introduced into a container 30 and cooled by water within the container.
活性炭は容器３０から水力で吸着反応炉に移送される。Activated carbon is hydraulically transferred from vessel 30 to the adsorption reactor.
幅狭の流動層２３内にて再生されるべき吸着剤は入口装
置２１を介して流動層２３内に導入され、図示されてい
ない出口装置を通過し再生された状態で流動層２３の他
端から排出される。The adsorbent to be regenerated in the narrow fluidized bed 23 is introduced into the fluidized bed 23 through the inlet device 21, passes through an outlet device (not shown), and leaves the other end of the fluidized bed 23 in the regenerated state. is discharged from.
流動層２３内に導入された吸着剤は、流動層２４内に導
入された活性炭より粒度の小さい活性炭とする。The adsorbent introduced into the fluidized bed 23 is activated carbon having a smaller particle size than the activated carbon introduced into the fluidized bed 24.
図面には流動層２３内に浸漬される邪魔板は示上の邪魔
板を装架し得ることは勿論である。Of course, the baffle plate shown in the drawing can be installed as the baffle plate immersed in the fluidized bed 23.
流動層２３に対する排出口（図示されていない）は容器
３１に連通し、再生された活性炭は流動層２３から容器
３１に導かれて容器内で水により冷却され、活性炭は容
器から水力で吸着反応炉に移流動層２３，２４を分離す
る隔壁２０は活性炭の装入口から排出口まで延在してい
ることに留意すべきである。A discharge port (not shown) for the fluidized bed 23 communicates with the container 31, and the regenerated activated carbon is led from the fluidized bed 23 to the container 31 and cooled by water in the container, and the activated carbon undergoes an adsorption reaction from the container by hydraulic power. It should be noted that the partition 20 separating the moving beds 23, 24 in the furnace extends from the activated carbon charge to the discharge.
流動層２３，２４の下方には有孔壁３３が配置されてい
る。A perforated wall 33 is arranged below the fluidized beds 23, 24.
２つの流動層２３，２４に対し必要とされる流動化ガス
は両流動層に対し共通の燃焼室２９内にて発生され、有
孔壁３３を通って各流動層内に上昇する。The fluidizing gas required for the two fluidized beds 23, 24 is generated in a combustion chamber 29 common to both fluidized beds and rises into each fluidized bed through a perforated wall 33.
両流動層２３，２４からの流動化ガスは同一の排気筒３
２を経て流動層反応装置から排出され、排出された流動
化ガスは後で燃焼される。The fluidized gas from both fluidized beds 23 and 24 is sent to the same exhaust stack 3.
2, and the discharged fluidizing gas is later combusted.
本発明による単一レベルの流動層反応装置の作動が実施
例について説明されるが、これは本発明を何等限定する
ものではない。The operation of a single level fluidized bed reactor according to the invention will be described by way of example, but this is not intended to limit the invention in any way.
例２
１１００ｇ／ｍ３のフェノール含有量を有する毎時３０
ｃｍ３のコークス製造廃水が浄化されるものとする。Example 2 30 per hour with a phenol content of 1100 g/m3
cm3 of coke production wastewater shall be purified.
浄化は一組となった２つの別々の吸着器内にて行われ、
吸着器はそれぞれ粒度１．５〜２．０ｍｍの活性炭２５
Ｏｋｇ／ｈおよび粒度０．５〜０．８ｍｍの活性炭６０
ｋｇ／ｈを必要とする。Purification takes place in a set of two separate adsorbers,
Each adsorber is made of activated carbon 25 with a particle size of 1.5 to 2.0 mm.
Activated carbon 60 with Okg/h and particle size 0.5-0.8mm
kg/h is required.
大きい方の粒度を有する活性炭の再生は長さ２．８ｍ，
幅０． ５５ｍを有する流動層内にて行われ、小さい方
の粒度を有する活性炭の再生は長さ２．８ｍ、幅０．１
５ｍを有する流動層内にて行われる。Regeneration of activated carbon with larger particle size is 2.8 m long,
Width 0. The regeneration of activated carbon with the smaller particle size is carried out in a fluidized bed with a length of 2.8 m and a width of 0.1 m.
It is carried out in a fluidized bed with a diameter of 5 m.
酸素を含まず且つ１１００℃の温度を有する流動化ガス
の１５００ｍ３／ｈが両流動層に共通の燃焼室内にて発
生され、流動化ガスは流動層下方に配置された有孔壁に
おいて各流動層下方にある異なる自由流通断面積に応じ
て２つの流動層に分配される。1500 m3/h of fluidizing gas, which is oxygen-free and has a temperature of 1100° C., is generated in a combustion chamber common to both fluidized beds, and the fluidized gas is distributed to each fluidized bed in a perforated wall located below the fluidized bed. It is distributed into two fluidized beds depending on the different free flow cross sections below.
流動化ガスは、１００ｍ３／ｈが幅の狭い流動層に入り
残りの１４００ｍ３／ｈが幅の広い流動層に入るように
分配される。The fluidizing gas is distributed such that 100 m3/h enters the narrow fluidized bed and the remaining 1400 m3/h enters the wide fluidized bed.
２つの流動層からの流動化ガス廃気は合体されて後で燃
焼される。The fluidizing gas waste gases from the two fluidized beds are combined and later combusted.
第１図は本発明による流動層反応装置の１実施例の概略
的縦断面図、第２図は第１図の流動層反応装置の平面図
、第３図は本発明による流動層反応装置の別の実施例の
概略的縦断面図、第４図は椰３図の流動層反応装置の平
面図である。
１，７，２３，２４・・・・・・流動層、５，８，２１
，２２・・・・・・装入口、６，１２，２８・・・・・
・堰、１３，２９・・・・・・燃焼室、１８，１９，３
３・・・・・・有孔壁、２，３，４，９，１０，１１，
２５，２６，２７・・・・・・邪魔板。FIG. 1 is a schematic longitudinal sectional view of an embodiment of the fluidized bed reactor according to the present invention, FIG. 2 is a plan view of the fluidized bed reactor of FIG. 1, and FIG. 3 is a schematic longitudinal sectional view of an embodiment of the fluidized bed reactor according to the present invention. A schematic longitudinal sectional view of another embodiment, FIG. 4 is a plan view of a fluidized bed reactor shown in FIG. 1, 7, 23, 24...Fluidized bed, 5, 8, 21
, 22...Charging port, 6, 12, 28...
・Weir, 13, 29... Combustion chamber, 18, 19, 3
3... Perforated wall, 2, 3, 4, 9, 10, 11,
25, 26, 27...Baffle board.
Claims (1)
れた粒状吸着剤を再生する方法にして、異なる吸着剤の
一方の第１分量を第１再生帯域に導入し異なる吸着剤の
他方の第２分量を第１再生帯域と共通の再生室内に配置
され第１再生帯域とは別個の第２再生帯域に導入する段
階と、前記別個の第１、第２再生帯域内にある吸着剤の
１方および他方の第１、第２分量を通して高温の再生ガ
スを通過させ異なる汚染された吸着剤を流動化し且つ再
生する段階と、再生された吸着剤の前記第１、第２分量
をそれぞれの再生帯域から取出す段階と、異なる吸着剤
の前記第１、第２分量を通過し終ったガスをそれぞれの
再生帯域から排除する段階と、を包含する特性及び／又
は粒度の異なる少くとも２つの汚染された粒状吸着剤を
再生する方法。1 A method of regenerating at least two contaminated particulate adsorbents of different properties and/or particle sizes, wherein a first amount of one of the different adsorbents is introduced into a first regeneration zone and a second amount of the other of the different adsorbents is introducing an amount of adsorbent into a second regeneration zone located within a regeneration chamber common to the first regeneration zone and separate from the first regeneration zone; and passing hot regeneration gas through the first and second volumes of the other to fluidize and regenerate the different contaminated adsorbents; and transferring the first and second volumes of regenerated adsorbent to respective regeneration zones. and rejecting from the respective regeneration zones the gases that have passed through the first and second portions of different adsorbents. How to regenerate granular adsorbents.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19752526714 DE2526714C2 (en) | 1975-06-14 | Fluidized bed reactor for the thermal regeneration of loaded adsorbents |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS51151270A JPS51151270A (en) | 1976-12-25 |
| JPS587339B2 true JPS587339B2 (en) | 1983-02-09 |
Family
ID=5949159
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP50130581A Expired JPS587339B2 (en) | 1975-06-14 | 1975-10-31 | KiyuuchiyakusaretakiyuuchiyakuzainonetsuTexaiseinotamenokariyusouhannouro |
Country Status (6)
| Country | Link |
|---|---|
| JP (1) | JPS587339B2 (en) |
| FI (1) | FI64749C (en) |
| FR (1) | FR2313975A1 (en) |
| GB (1) | GB1493096A (en) |
| IT (1) | IT1061616B (en) |
| SE (1) | SE421674B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53129175A (en) * | 1977-04-18 | 1978-11-10 | Daikin Ind Ltd | Continuous adsorber using active carbon |
| ZA793953B (en) * | 1978-08-08 | 1980-08-27 | Coal Industry Patents Ltd | Heat treatment of material |
| GB2114555B (en) * | 1982-01-22 | 1985-03-13 | Coal Ind | Improvements in the regeneration of adsorbents |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4932432A (en) * | 1972-07-24 | 1974-03-25 |
-
1975
- 1975-10-31 JP JP50130581A patent/JPS587339B2/en not_active Expired
-
1976
- 1976-05-31 IT IT4972376A patent/IT1061616B/en active
- 1976-06-11 SE SE7606700A patent/SE421674B/en not_active IP Right Cessation
- 1976-06-14 FR FR7617982A patent/FR2313975A1/en active Granted
- 1976-06-14 GB GB2448376A patent/GB1493096A/en not_active Expired
- 1976-06-14 FI FI761707A patent/FI64749C/en not_active IP Right Cessation
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4932432A (en) * | 1972-07-24 | 1974-03-25 |
Also Published As
| Publication number | Publication date |
|---|---|
| DE2526714A1 (en) | 1976-12-09 |
| DE2526714B1 (en) | 1976-12-09 |
| FI64749C (en) | 1984-01-10 |
| IT1061616B (en) | 1983-04-30 |
| SE7606700L (en) | 1976-12-15 |
| SE421674B (en) | 1982-01-25 |
| GB1493096A (en) | 1977-11-23 |
| JPS51151270A (en) | 1976-12-25 |
| FR2313975B1 (en) | 1978-05-19 |
| FI64749B (en) | 1983-09-30 |
| FR2313975A1 (en) | 1977-01-07 |
| FI761707A (en) | 1976-12-15 |
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