JPS6158212B2 - - Google Patents
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- Publication number
- JPS6158212B2 JPS6158212B2 JP53124095A JP12409578A JPS6158212B2 JP S6158212 B2 JPS6158212 B2 JP S6158212B2 JP 53124095 A JP53124095 A JP 53124095A JP 12409578 A JP12409578 A JP 12409578A JP S6158212 B2 JPS6158212 B2 JP S6158212B2
- Authority
- JP
- Japan
- Prior art keywords
- desorption
- gas
- zone
- temperature
- adsorbent
- 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.)
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Links
- 238000003795 desorption Methods 0.000 claims description 107
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 56
- 238000001179 sorption measurement Methods 0.000 claims description 39
- 239000003463 adsorbent Substances 0.000 claims description 30
- 238000001816 cooling Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 5
- 230000007423 decrease Effects 0.000 claims description 4
- 238000003303 reheating Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 73
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 17
- 239000000126 substance Substances 0.000 description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 238000000034 method Methods 0.000 description 10
- 238000000926 separation method Methods 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000004821 distillation Methods 0.000 description 3
- 239000000835 fiber Substances 0.000 description 3
- 239000008187 granular material Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000002336 sorption--desorption measurement Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229920002972 Acrylic fiber Polymers 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000010000 carbonizing Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000003566 sealing material Substances 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 150000008282 halocarbons Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 239000004745 nonwoven fabric Substances 0.000 description 1
- 235000019645 odor Nutrition 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 239000003021 water soluble solvent Substances 0.000 description 1
Description
【発明の詳細な説明】
本発明は、ガス中の特定の成分を活性炭に吸着
させて分離除去する技術の改良に関し、閉塞系内
において吸着一脱着を連続して実施できるうにし
た装置に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an improvement in technology for separating and removing specific components in a gas by adsorbing them onto activated carbon, and relates to an apparatus that can perform adsorption and desorption continuously in a closed system.
種々の化学的工程から出る廃ガスや作業雰囲気
中に含まれている有害成分を除去する目的で、し
ばしば活性炭による吸着が利用されている。活性
炭吸着はまた比較的低濃度であるが有毒であつた
り、悪臭を伴うような物質の除去に、とくに有効
である。 Activated carbon adsorption is often used to remove harmful components contained in waste gases and working atmospheres from various chemical processes. Activated carbon adsorption is also particularly effective in removing relatively low concentrations of toxic or malodorous substances.
従来用いられて来た活性炭は、ほとんどが粒状
（顆粒状または粉末状）である。その利用法は、
被処理ガスとの接触のさせ方から、固定層式と流
動層式とに大別される。活性炭は与えられた条件
において吸着平衡に近づくにつれて吸着能力が低
下するのに、ごく少規模の場合を別にすれば、脱
着操作により吸着物質を除いて再賦活し、くり返
し使用するのがふつうである。従つて、固定層式
では少なくとも２個の容器を用意し、一定時間ご
とに吸着と脱着とを切換える。この脱着には相当
の長時間を要し、全体として装置は大きくなり、
吸着材の使用量も多くなる。流動層式は、回分式
で実施できることはもちろん、連続化も可能では
あるが、被処理ガスの流速を最少流動速度以上に
保たなければならないので圧力損失が大きく、吸
着材の使用効率がそれほど高くない割には損耗が
激しいこともあつて、設備費、運転費ともに嵩
む。両者の折衷的な方式として、吸着材と被処理
ガスとの接触効果を高める狙いで吸着材を移動層
とすること、たとえば回転移動の方式なども発表
されているが、機械的に複雑になるので、それに
伴う問題は避けられない。 Most of the conventionally used activated carbons are in the form of granules (granules or powders). Its usage is
Depending on the method of contact with the gas to be treated, it is broadly divided into fixed bed type and fluidized bed type. Although activated carbon's adsorption capacity decreases as it approaches adsorption equilibrium under given conditions, except in very small-scale cases, it is common to remove adsorbed substances through a desorption operation, reactivate it, and use it repeatedly. . Therefore, in the fixed bed type, at least two containers are prepared, and adsorption and desorption are switched at regular intervals. This attachment and detachment takes a considerable amount of time, and the overall size of the device increases.
The amount of adsorbent used also increases. The fluidized bed method can be carried out batchwise as well as continuously, but the flow rate of the gas to be treated must be kept above the minimum flow rate, resulting in a large pressure loss and the efficiency of using the adsorbent is not so high. Although it is not expensive, it is subject to heavy wear and tear, which increases both equipment and operating costs. As a compromise between the two, methods have been announced in which the adsorbent is used as a moving layer, such as a rotational movement method, with the aim of increasing the contact effect between the adsorbent and the gas to be treated, but this method becomes mechanically complex. Therefore, the problems associated with it are inevitable.
前述のように、活性炭からの被吸着物質の脱着
は必らずしも容易ではなく、通常は過熱水蒸気を
吹き込んで加熱することにより強力に脱着するこ
とが行なわれる。しかし、被吸着物質が水溶性の
もの、たとえばアルコールやケントのような水溶
性有機溶剤などの場合には、脱着させた後に凝縮
した水溶液からこの物質を分離するため、さらに
蒸留などの操作が必要となる。吸着材の固定層中
に予め加熱用コイルを設けておき、間接加熱によ
つてこの問題を避けることも試みられたが、脱着
が不完全であるため吸着材の使用効率がよくない
という悩みはなくならない。 As mentioned above, desorption of adsorbed substances from activated carbon is not always easy, and powerful desorption is usually carried out by heating the activated carbon by blowing in superheated steam. However, if the substance to be adsorbed is water-soluble, for example a water-soluble organic solvent such as alcohol or Kent, further operations such as distillation are required to separate the substance from the condensed aqueous solution after desorption. becomes. Attempts have been made to avoid this problem by installing a heating coil in advance in the fixed bed of adsorbent and using indirect heating, but this problem has resulted in the inefficient use of the adsorbent due to incomplete desorption. It won't go away.
本発明は、上述した諸問題を解決すべく行なつ
た活性炭吸着技術の改良研究の成果である。とく
に本発明においては、近年開発された繊維状活性
炭のシートを利用するとき、そのすぐれた脱着性
と低いガスの通過抵抗により、顕著な効果を奏す
る。 The present invention is the result of research to improve activated carbon adsorption technology in order to solve the above-mentioned problems. In particular, in the present invention, when a sheet of fibrous activated carbon, which has been developed in recent years, is used, remarkable effects are achieved due to its excellent desorption properties and low gas passage resistance.
本発明の目的は、活性炭を用いてガス中の特定
の成分を吸着除去する装置であつて、下記の利点
を有するものを提供することにある。 An object of the present invention is to provide an apparatus for adsorbing and removing specific components in gas using activated carbon, which has the following advantages.
(イ) 脱着が容易に行なわれるため閉塞系内で吸着
−脱着を連続的に実施することができ、しかも
それに要する吸着材が少量で済むこと、
(ロ) 被処理ガスの圧力損失が低く、従つて動力消
費が少ないこと、
(ハ) 過熱水蒸気による脱着を行なわず、従つて水
溶性物質の吸着−脱着の後にもそれと凝縮水と
の分離に蒸留等の操作を必要としないこと、
(ニ) 被処理ガス中の吸着すべき物質の濃度が変動
したときにも、その除去率を一定にできる（残
存量を一定値に抑える）こと、
(ホ) 吸着材の全部または一部の交換が従来技術よ
り容易に行なえること。(b) Since desorption is easy, adsorption-desorption can be carried out continuously in a closed system, and only a small amount of adsorbent is required; (b) The pressure loss of the gas to be treated is low; Therefore, power consumption is low; (c) desorption using superheated steam is not performed, and therefore, even after adsorption-desorption of water-soluble substances, operations such as distillation are not required to separate condensed water from water-soluble substances; ) Even when the concentration of the substance to be adsorbed in the gas to be treated fluctuates, the removal rate can be kept constant (residual amount kept at a constant value); (e) All or part of the adsorbent can be replaced. Easier to perform than conventional techniques.
上記の目的を達成する、連続的な閉塞系内で吸
着−脱着方法を実施するための装置は、次の基本
的部分から構成される。すなわち、
〇 活性炭に被処理ガスを接触させてその中の特
定の成分を吸着させる吸着ゾーンと、この吸着
後の活性炭に高温の脱着用ガスを作用させて吸
着されている成分を脱着させる脱着ゾーン、お
よび両者の中間にあつて吸着材の移動は許すが
両ゾーンの雰囲気はガスのカーテンにより遮断
するはたらきをするガスシールゾーン、
〇 上記三つのゾーンを一体におおうチヤンバ
ー、
〇 活性炭の吸着材を無端ベルト状の多孔ケース
に収容したもの、
〇 上記の吸着材入り無端ベルトを吸着ゾーンと
脱着ゾーンとの間を循環的に移動させる駆動手
段、
〇 脱着後の脱着ガスからその中に含まれている
成分を分離する手段、および
〇 上記成分を分離した脱着用ガスを再び脱着ゾ
ーンに循環させる手段、である。 The apparatus for carrying out the adsorption-desorption process in a continuous closed system, which achieves the above objectives, consists of the following basic parts: That is, 〇 An adsorption zone in which activated carbon is brought into contact with a gas to be treated to adsorb specific components therein, and a desorption zone in which high-temperature desorption gas is applied to the activated carbon after adsorption to desorb the adsorbed components. , and a gas seal zone that is located between the two and allows the movement of the adsorbent but blocks the atmosphere in both zones with a gas curtain; 〇 A chamber that covers the above three zones as one; 〇 An activated carbon adsorbent. A drive means for cyclically moving the endless belt containing the adsorbent between the adsorption zone and the desorption zone; A drive means for cyclically moving the endless belt containing the adsorbent between the adsorption zone and the desorption zone; and (0) means for circulating the desorption gas from which the above components have been separated back into the desorption zone.
本発明において吸着材として使用する活性炭と
しては、有機物の繊維を炭化処理することによつ
て得られる繊維状活性炭がとくに好適である。 As the activated carbon used as an adsorbent in the present invention, fibrous activated carbon obtained by carbonizing organic fibers is particularly suitable.
シート状に成形した繊維状活性炭は、有機物の
繊維をまず布、不織布またはフエルト状に加工し
たのち炭化することによつて、好都合に製造され
る。本発明にとつては、近年開発された、アクリ
ル繊維を原料とし、これを特殊な条件下に炭化し
て活う戦としたものが最適である。このアクリル
繊維を原料とする繊維状活性炭は、一般の活性炭
と異なつて、原料に由来する窒素を数％（炭化処
理条件によつて若干の差異がある）含有してお
り、そのため塩基的性質を有する。従つて酸性の
物質、たとえば悪臭の原因となることの多い硫化
水素およびメルカプタン類の吸着除去に、とくに
有効である。そのほか、アルコール、アルデヒ
ド、ケトン、エステルあるいはハロゲン化炭化水
素など、従来の活性炭ではどちらかといえば不向
きであつた極性の化合物の吸着能力も高い。一
方、塩基性物質の吸着量も、従来の活性炭に劣る
わけではない。従つて本発明のこの態様は、酸性
の物質および中性であつて極性の高い物質にの吸
着にとくに有利であるほか、塩基性の物質対して
も不利はなく適用できる。 Fibrous activated carbon formed into sheets is conveniently produced by first processing organic fibers into cloth, non-woven fabric or felt and then carbonizing them. For the present invention, the most suitable method is one that uses acrylic fiber as a raw material and carbonizes it under special conditions, which has been developed in recent years. Unlike ordinary activated carbon, this fibrous activated carbon made from acrylic fibers contains several percent of nitrogen derived from the raw material (slight differences depending on the carbonization treatment conditions), and therefore has basic properties. have Therefore, it is particularly effective in adsorbing and removing acidic substances, such as hydrogen sulfide and mercaptans, which often cause bad odors. In addition, it has a high ability to adsorb polar compounds, such as alcohols, aldehydes, ketones, esters, and halogenated hydrocarbons, for which conventional activated carbon is rather unsuitable. On the other hand, the adsorption amount of basic substances is not inferior to that of conventional activated carbon. Therefore, this aspect of the present invention is particularly advantageous for adsorption to acidic substances and neutral and highly polar substances, and can also be applied to basic substances without any disadvantages.
吸着材である活性炭は、粒状のものはもちろ
ん、シート状に成形した繊維状のものであつて
も、それ自体だけでは機械的強度が十分でないの
で、多孔ケースに収容して無端ベルトを形成す
る。これには上下面が金網または多孔板で通気性
をもち、両側面が気密である適宜の寸法のカート
リツジを多数用意し、その前後端を実質上気密な
丁番により連結して無端ベルトとすることが推奨
される。 Activated carbon, which is an adsorbent, does not have sufficient mechanical strength on its own, whether it is in the form of granules or fibers formed into sheets, so it is placed in a porous case to form an endless belt. . For this purpose, prepare a large number of cartridges of appropriate dimensions, with the upper and lower surfaces made of wire mesh or perforated plates for ventilation, and both sides airtight, and connect the front and rear ends with a substantially airtight hinge to form an endless belt. It is recommended that
これらは案内とガスシールを兼ねるレール上
を、スプロケツト方式により駆動するとよい。 These are preferably driven by a sprocket system on a rail that serves as both a guide and a gas seal.
脱着は、吸着ゾーンから来る吸着材に、被処理
ガスより高温のガスを適用することによつて行な
う。脱着用ガスは不活性ガス、たとえば窒素や窒
素と炭酸ガスとの混合物を使用するとよいが、工
程にとつて不都合でない限り、任意にえらぶこと
ができ、たとえば吸着される成分が可燃性でなけ
れば、空気を使用することもできる。 Desorption is carried out by applying a gas hotter than the gas to be treated to the adsorbent coming from the adsorption zone. As the desorption gas, it is preferable to use an inert gas, such as nitrogen or a mixture of nitrogen and carbon dioxide gas, but it can be arbitrarily selected as long as it is not inconvenient for the process. For example, if the component to be adsorbed is not flammable, , air can also be used.
脱着により吸着材から離れた成分は、脱着ガス
と一体となつて分離手段に入り、そこで脱着用ガ
スから分けられる。この分離手段としては、特定
の成分が容易に液化する物質であるときは、冷却
による凝縮を好都合に利用できる。分離後のガス
は再び脱着ゾーンに送り返して脱着に使用する
が、冷却をした場合には必要な温度まで再加熱す
る必要がある。冷却による分離は吸着される成分
が有機溶剤であるようなときに有利であつて、と
くに水溶性溶剤である場合も凝縮したものは（被
処理ガスの湿度により若干の影響はあるものの）
ほとんど無水の状態で得られ、前述したように蒸
留などの水との分離工程を必要とせずに回収利用
できる。 The components separated from the adsorbent by desorption enter the separation means together with the desorption gas, where they are separated from the desorption gas. As this separation means, when the specific component is a substance that easily liquefies, condensation by cooling can be advantageously used. The separated gas is sent back to the desorption zone and used for desorption, but if it is cooled, it must be reheated to the required temperature. Separation by cooling is advantageous when the component to be adsorbed is an organic solvent, especially when the component is a water-soluble solvent and is condensed (although it may be slightly affected by the humidity of the gas to be treated).
It is obtained in an almost anhydrous state, and as mentioned above, it can be recovered and used without the need for a separation process from water such as distillation.
吸着条件は、周知のとおり最終的には吸着平衡
によつて決定され、それは温度および圧力（被吸
着物質の濃度）の関数である。実際上は平衡に近
づくに要する時間が問題となることが多く、理論
吸着量の何％を利用できるかは、場合によつて異
なる。低温ほど有利であるから、必要があれば被
処理ガスを多少冷却して吸着ゾーンに送り込むこ
とも実際的である。 As is well known, the adsorption conditions are ultimately determined by the adsorption equilibrium, which is a function of temperature and pressure (concentration of the adsorbed substance). In practice, the time required to approach equilibrium is often a problem, and what percentage of the theoretical adsorption amount can be utilized varies depending on the case. Since lower temperatures are more advantageous, it is practical to cool the gas to be treated to some extent before sending it to the adsorption zone, if necessary.
一方、脱着は高温ほど強く行なわれるので脱着
用ガスはなるべく高温で供給することが望まし
い。ところが特定の成分の分離手段として冷却に
よる凝縮を行なつた場合には、高温にするほど再
加熱に要する熱量は多くなる。脱着ガスの冷却温
度をあまり低くとらなければこの熱量は少なくて
済むが、分離後の脱着用ガス中に含まれる特定の
成分の濃度が高くなることは避けられず、これは
脱着平衡に不利に作用して、吸着ゾーンに循環す
る吸着材に残留する成分の量を多くし、吸着能力
を低下させる結果となる。こりようなわけで、脱
着の温度および冷却の温度ならびに脱着用ガスの
循環量は、与えられた条件を総合的に検討して決
定すべきである。 On the other hand, since desorption is performed more strongly at higher temperatures, it is desirable to supply the desorption gas at as high a temperature as possible. However, when condensation by cooling is used as a means for separating specific components, the higher the temperature, the more heat is required for reheating. This amount of heat can be reduced if the cooling temperature of the desorption gas is not too low, but it is inevitable that the concentration of certain components contained in the desorption gas after separation will increase, which is detrimental to the desorption equilibrium. This results in an increase in the amount of components remaining in the adsorbent circulating in the adsorption zone, resulting in a decrease in adsorption capacity. Therefore, the desorption temperature, the cooling temperature, and the amount of circulation of the desorption gas should be determined by comprehensively considering the given conditions.
吸着除去すべき特定の成分がエタノールであ
り、その濃度が空気中０〜5000ppmの範囲にあ
る場合に例をとると、吸着は40℃以下、好ましく
は30℃またはそれ以下の温度で行ない、脱着用ガ
スとしては窒素を用いてその温度を100℃〜250℃
とし、脱着ガスを60℃以下に冷却してエタノール
の大部分を凝縮させ回収するといつた条件が代表
的である。 For example, if the specific component to be adsorbed and removed is ethanol and its concentration is in the range of 0 to 5000 ppm in air, the adsorption is carried out at a temperature below 40°C, preferably 30°C or below, and the desorption Nitrogen is used as the gas and the temperature is 100℃~250℃.
Typical conditions include cooling the desorbed gas to below 60°C to condense and recover most of the ethanol.
上述のガスシールゾーンに用いるガスは、脱着
用ガスに関して述べたと同様の意味で不活性なガ
スであればよく、脱着に用いるものと同じであつ
ても異なるものであつてもよいが、操業中に少し
ずつではあるが起る両者の混合を考慮すると、同
種のものがよい。 The gas used in the gas seal zone described above may be any inert gas in the same sense as described for the desorption gas, and may be the same or different from that used for desorption, but Considering that mixing of the two occurs little by little, it is better to use the same type of material.
脱着ガス中に含まれて来る成分を凝縮により分
離する場合は、そのためのコンデンサすなわちク
ーラとガス一液セパレータの組みを設けるととも
に、温度の低下した脱着用ガスを脱着ゾーンに送
り返すに先立つて再加熱するヒータを設ける。上
記の脱着ガスの冷却と成分分離後の脱着用ガスの
加熱のためには、熱交換器をおいて両者の間で熱
交換させることが推奨される。もちろん、これに
加えて冷却および加熱をすることは当然に必要で
はあるがエネルギー消費の節約には役立つ。 If the components contained in the desorption gas are to be separated by condensation, a combination of a condenser or cooler and a gas-liquid separator is installed, and the desorption gas, whose temperature has dropped, is reheated before being sent back to the desorption zone. A heater will be installed. In order to cool the desorption gas and heat the desorption gas after component separation, it is recommended to install a heat exchanger to exchange heat between the two. Of course, cooling and heating in addition to this are naturally necessary but help save energy consumption.
熱エネルギー利用の強化と工程の一層の効率化
を意図するときは、脱着ゾーンを比較的高温で操
作する脱着室と、比較的低温で操作する脱着室と
に分けることが望ましい。上記の熱交換により加
熱された、比較的低温の脱着用ガスがまず低温の
脱着室に入り、一旦そこを出てからヒータにより
高温に加熱されたのち高温の脱着室に入るように
配管系統を用意する。吸着ゾーンから移動してき
た、特定の成分を吸着している吸着材は、はじめ
低温の脱着室において予熱されたのち高温の脱着
室に移り、そこで大部分の脱着が行なわれる。次
に再び低温の脱着室に入り、比較的低温であるが
成分濃度の低い脱着用ガスと接触して脱着を完了
しガスを温めるとともに、自身は温度が低下して
次の吸着に好都合な状態となつて、再び吸着ゾー
ンに戻るように構成するわけである。 When it is intended to enhance thermal energy utilization and make the process more efficient, it is desirable to divide the desorption zone into a desorption chamber that operates at relatively high temperatures and a desorption chamber that operates at relatively low temperatures. The piping system is designed so that the relatively low-temperature desorption gas heated by the above heat exchange first enters the low-temperature desorption chamber, leaves there, is heated to a high temperature by a heater, and then enters the high-temperature desorption chamber. prepare. The adsorbent adsorbing a specific component that has moved from the adsorption zone is first preheated in a low-temperature desorption chamber and then transferred to a high-temperature desorption chamber, where most of the desorption takes place. Next, it enters the low-temperature desorption chamber again, and comes into contact with the desorption gas, which is relatively low temperature but has a low concentration of components, to complete desorption and warm the gas, while the temperature of the gas itself decreases, creating a state favorable for the next adsorption. Therefore, the structure is such that it returns to the adsorption zone again.
空気中のエタノールの吸着除去の例のように可
燃性のものを取扱う場合は爆発の危険防止の観点
から、高濃度のエタノールの存在する脱着ゾーン
中に空気が混入することを避ける必要がある。こ
れには、脱着ゾーンの圧力を吸着ゾーンの圧力よ
り僅かに高くして操業するとよい。脱着用ガスお
よびシール用のガスは一部吸着ゾーンに押しやら
れて損失となるので、補給する必要がある。 When handling flammable materials, such as the adsorption removal of ethanol from the air, it is necessary to prevent air from entering the desorption zone where high concentrations of ethanol are present, in order to prevent the risk of explosion. This can be achieved by operating the desorption zone at a slightly higher pressure than the adsorption zone. Some of the desorption gas and sealing gas are pushed to the adsorption zone and are lost, so they must be replenished.
被処理ガス中の吸着除去すべき成分の濃度が経
時的に変化する場合が、実際の装置において少な
くない。それにも拘らず処理後のガス中のその成
分の濃度を一定値以下に抑えることがしばしば要
求され、そのような要求にこたえるためには、吸
着材の循環速度を変えればよい。どの程度の濃度
増加に対してどのくらい循環速度を高めるべきか
を予め測定しておき、変化に自動的に追従させる
ことが望ましい。 In actual equipment, there are many cases in which the concentration of the component to be adsorbed and removed in the gas to be treated changes over time. Nevertheless, it is often required to suppress the concentration of the component in the treated gas below a certain value, and in order to meet such a requirement, the circulation speed of the adsorbent can be varied. It is desirable to measure in advance how much the circulation rate should be increased in response to an increase in concentration, and to automatically follow the change.
上述した装置の一例の概要を第１図に示す。 FIG. 1 shows an outline of an example of the above-mentioned apparatus.
被処理ガスは、発生源Ａから、必要によりクー
ラ５を通して所定の温度に冷却されて、チヤンバ
１内の吸着ゾーン２に入り、ここで吸着材を収容
したカートリツジ２１を連結して成る無端ベルト
６を通過し、ガス中に含まれている特定の成分を
吸着除去される。無害になつたガスは、Ｂから大
気中に放出される。（このガスに対してさらに別
の処理を行なうときは、そのための装置へ導
く。）
無端ベルト６は、スプロケツトギア７，７′に
より駆動され、ガスシールゾーン３を通つて脱着
ゾーン４に送られる。シールゾーン３にはブロア
８により窒素ガスが循環し、ガスカーテンを形成
して左右のゾーンを遮断している。損失ガスは、
窒素源Ｃから補給する。 The gas to be treated is cooled from the source A to a predetermined temperature through a cooler 5 if necessary, and then enters the adsorption zone 2 in the chamber 1, where it is passed through an endless belt 6 that connects cartridges 21 containing adsorbents. through which specific components contained in the gas are adsorbed and removed. The now harmless gas is released from B into the atmosphere. (When further processing is performed on this gas, it is directed to a device for that purpose.) The endless belt 6 is driven by sprocket gears 7 and 7' and is sent through the gas seal zone 3 to the desorption zone 4. It will be done. Nitrogen gas is circulated in the seal zone 3 by a blower 8, forming a gas curtain to block off the left and right zones. Loss gas is
Replenish from nitrogen source C.
脱着ゾーン４における活性炭と脱着用ガスとの
接触は、比較的高温の４Ｂおよび４B′ならびに比
較的低温の４Ａおよび４A′の四つの脱着室内に
おいて行なわれる。これらの脱着室は、カートリ
ツジの流れを上下からはさむように小室を形成し
たものであつて、各室に送られて来る脱着用ガス
および脱着ガスが他の室に混入して脱着効率の低
下をもたらすのを防止するばかりでなく、脱着用
ガスの適当な線速度を維持するはたらきをする。
この小室は、各脱着室ごとに必要により複数個ず
つ設ける。 The contact between the activated carbon and the desorption gas in the desorption zone 4 takes place in four desorption chambers, 4B and 4B' at relatively high temperatures and 4A and 4A' at relatively low temperatures. These desorption chambers are formed into small chambers sandwiching the flow of cartridges from above and below, and prevent the desorption gas and desorption gas sent to each chamber from getting mixed into other chambers and reducing the desorption efficiency. It not only prevents the desorption from occurring, but also serves to maintain a suitable linear velocity of the desorption gas.
A plurality of these small chambers are provided for each desorption chamber, if necessary.
吸着ゾーン２から脱着ゾーン４の脱着室４
A′に移つた吸着材は、比較的低温の脱着用ガス
で予熱され、続いて脱着室４B′および４Ｂにおい
て、ヒータ９で十分な高温に加熱されてくる脱着
用ガスにより吸着成分の脱着が完了し、脱着室４
Ａにおいて比較的低温の脱着用ガスで若干冷やさ
れ、再び脱着のために吸着ゾーン２へ戻る。 Desorption chamber 4 from adsorption zone 2 to desorption zone 4
The adsorbent transferred to A' is preheated with a relatively low-temperature desorption gas, and then in the desorption chambers 4B' and 4B, the adsorbed components are desorbed by the desorption gas heated to a sufficiently high temperature by the heater 9. Completed, desorption room 4
At A, it is slightly cooled with a relatively low temperature desorption gas and returns to the adsorption zone 2 for desorption again.
成分の脱着後のガスは熱交換器１０を通つてク
ーラ１１に入り、成分の凝縮点以下の温度に冷却
され、セパレータ１２に導かれる。凝縮した成分
１３はＤに回収して可能ならば再利用する。この
成分と分離された脱着用ガスは、ブロア１４によ
り前記の熱交換器１０に送られ高温の脱着室４
B′からのガスにより温められ、低温の脱着室４
A′へ戻る。 The gas after the components have been desorbed passes through the heat exchanger 10 and enters the cooler 11, where it is cooled to a temperature below the condensation point of the components and guided to the separator 12. The condensed component 13 is recovered to D and reused if possible. The desorption gas separated from this component is sent to the heat exchanger 10 by the blower 14, and is sent to the high temperature desorption chamber 4.
The desorption chamber 4 is heated by the gas from B′ and is at a low temperature.
Return to A′.
吸着材の無端ベルト６を形成するカートリツジ
２１は、上面２２および下面２３がともに多孔板
であつてこの方向に通気性を有するケースを単位
とし、その前後を、丁番２４を用いて連結する。
側面２５にはスプロケツト方式で駆動するための
棒２６が設けてあり、またシール材２７が貼つて
あつて、レール２８，２９に沿つて移動する。こ
のケースの内部には、繊維状活性炭をシート状に
成形した吸着材３１が１枚ないし数枚収容されて
いる。これは必要に応じて交換可能である。 The cartridge 21 forming the endless belt 6 of adsorbent has a case unit whose upper surface 22 and lower surface 23 are both perforated plates and has air permeability in this direction, and the front and rear of the case are connected using a hinge 24.
A rod 26 for driving by a sprocket method is provided on the side surface 25, and a sealing material 27 is pasted to move along rails 28, 29. Inside this case, one or several sheets of adsorbent material 31 made of fibrous activated carbon formed into a sheet shape are housed. This can be replaced if necessary.
以上の説明から理解されるように、本発明に従
うときは、ガス中の有害成分の吸着除去に際して
連結操作が有利に実現する。脱着に水蒸気を必要
としないので、エネルギー消費が少ない上に排水
処理の問題もない。脱着用ガスは実質上いわゆる
クローズドシステムで利用されるから、二次公害
のおそれはなく、その損失は僅かであつて補給が
容易である。被処理ガスの通過および脱着用ガス
の循環に要する動力は、とくに繊維状活性炭を使
用したときはそのガス通過抵抗が低いため少量で
足り、この点からも省エネルギー操業が実現す
る。本発明の適用できる分野は極めて広範囲であ
る。 As can be understood from the above description, when the present invention is followed, the connection operation is advantageously realized when removing harmful components in gas by adsorption. Since no water vapor is required for desorption, energy consumption is low and there are no problems with wastewater treatment. Since the desorption gas is essentially used in a so-called closed system, there is no risk of secondary pollution, its loss is small, and it is easy to replenish. The power required for passage of the gas to be treated and circulation of the desorption gas is small, especially when fibrous activated carbon is used because its gas passage resistance is low, and from this point of view as well, energy-saving operation is realized. The fields of application of the present invention are extremely wide.
実施例
図面に示した装置を用いて、印刷作業の雰囲気
から発生する、エタノール最大5000ppmを含有
する空気を400m3／hrの割合で処理し、残存エタ
ノール量200ppm以下にして放出した。40℃の被
処理ガスを30℃に冷却して導入し、0.15m／sec
の速さで移動している厚さ90mmの繊維状活性炭フ
エルト層を通過させた。脱着は170℃の（窒素＋
炭酸ガス）を使用し、0.2m／secの流速で供給し
た。脱着後のガスを60℃に冷却してエタノールを
凝縮させ、実質上無水の状態で回収した。このエ
タノールは再使用可能であつた。Example Using the apparatus shown in the drawings, air containing a maximum of 5000 ppm of ethanol generated from the atmosphere of a printing operation was treated at a rate of 400 m 3 /hr to reduce the amount of residual ethanol to 200 ppm or less and release it. The gas to be treated at 40℃ is cooled to 30℃ and introduced at 0.15m/sec.
It passed through a layer of 90 mm thick fibrous activated carbon felt that was moving at a speed of . Desorption is performed at 170℃ (nitrogen +
Carbon dioxide gas) was used and supplied at a flow rate of 0.2 m/sec. The desorbed gas was cooled to 60°C to condense the ethanol and was recovered in a substantially anhydrous state. This ethanol was reusable.
図面は本発明の装置の一例を説明するためのも
のであつて、第１図は装置の概要を示す系統図で
あり、第２図は繊維状活性炭を収容した吸着材カ
ートリツジを連結して成る無端ベルトの、一部を
切欠いて断面を示した一部の側面図であり、第３
図はその平面図、第４図は第３図の―方向の
断面にレールを加えて示した図である。
１…チヤンバ、２…吸着ゾーン、３…ガスシー
ルゾーン、４…脱着ゾーン、４Ａ，４A′…低温
の脱着室、４Ｂ，４B′…高温の脱着室、５，１１
…クーラ、６…吸着材の無端ベルト、７，７′…
スプロケツトギア、８，１４…ブロア、９…ヒー
タ、１０…熱交換器、１２…セパレータ、１３…
凝縮成分、２１…カートリツジ、２２，２３…上
面、下面、２４…丁番、２５…側面、２６…駆動
用の棒、２７…シール材、２８，２９…レール、
３１…吸着材、Ａ…被処理ガス、Ｂ…放出ガス、
Ｃ…シールガス源、Ｄ…成分回収。
The drawings are for explaining an example of the device of the present invention, and FIG. 1 is a system diagram showing an overview of the device, and FIG. 2 is a system diagram showing an outline of the device, and FIG. FIG. 3 is a side view of a portion of the endless belt showing a cross section with a portion cut away;
The figure is a plan view thereof, and FIG. 4 is a cross-sectional view taken in the - direction of FIG. 3 with rails added. 1...Chamber, 2...Adsorption zone, 3...Gas seal zone, 4...Desorption zone, 4A, 4A'...Low temperature desorption chamber, 4B, 4B'...High temperature desorption chamber, 5, 11
...Cooler, 6...Endless belt of adsorbent, 7,7'...
Sprocket gear, 8, 14...Blower, 9...Heater, 10...Heat exchanger, 12...Separator, 13...
Condensed component, 21... Cartridge, 22, 23... Top surface, bottom surface, 24... Hinge, 25... Side surface, 26... Driving rod, 27... Sealing material, 28, 29... Rail,
31... Adsorbent, A... Gas to be treated, B... Released gas,
C... Seal gas source, D... Component recovery.
Claims (1)
的に吸着し続いて脱着することによりガスから分
離除去する装置であつて、 活性炭に被処理ガスを接触させてその中の特定
の成分を吸着させる吸着ゾーンと、この吸着後の
活性炭に高温の脱着用ガスを作用させて吸着され
ている成分を脱着させる脱着ゾーンとが、中間の
ガスシールゾーンを介して一つのチヤンバー内に
存在し、 その中において吸着材が無端ベルト状の多孔ケ
ースに収容されて、上記吸着ゾーンと脱着ゾーン
とを循環的に移動するよう設けられ、さらに、 脱着後の脱着ガスからその中に含まれている成
分を分離する手段およびこの成分を分離した脱着
用ガスを再び脱着ゾーンに循環させる手段とを備
えて成る装置。 ２ 吸着材が所定の寸法のシート状に成形された
繊維状活性炭であつて、これを１枚ないし数枚重
ねて収容した上下の面が通気性のカートリツジを
多数丁番により連結して無端ベルトを形成し、こ
れをスプロケツト方式により駆動してガスシール
を兼ねるレール上を移動させるように構成した特
許請求の範囲第１項の装置。 ３ 脱着ガス中に含まれている成分を分離する手
段がコンデンサであり、コンデンサを出た脱着用
ガスを脱着ゾーンに循環させる途中でこれを再加
熱する手段を備えた特許請求の範囲第１項の装
置。 ４ 脱着ゾーンからの脱着後のガスと、コンデン
サにおいて凝縮した成分を分離した後の脱着用の
ガスとの間で熱交換を行ない、前者を冷却すると
ともに後者を加熱する特許請求の範囲第３項の装
置。 ５ 脱着ゾーンが比較的低温の脱着室と比較的高
温の脱着室を有し、上記熱交換により加熱された
比較的低温の脱着用ガスがまず低温の脱着室に入
り、一旦そこを出てからヒータにより比較的高温
に加熱されたのち高温の脱着室に入るよう配管さ
れ、吸着ゾーンから移動してきた特定の成分を吸
着した吸着材がはじめ低温の脱着室において予熱
されたのち高温の脱着室に移つてそこで大部分の
脱着が行なわれ、次に再び低温の脱着室に入つて
低温の脱着用ガスを温め脱着を完了するととも
に、自身の温度は低下して吸着ゾーンに戻るよう
に構成した特許請求の範囲第４項の装置。 ６ 脱着ゾーンの圧力を吸着ゾーンのそれより僅
かに高く保つた端許請求の範囲第１項の装置。[Claims] 1. A device for separating and removing specific components in a gas by continuously adsorbing and then desorbing them using activated carbon, which comprises: An adsorption zone that adsorbs specific components in the activated carbon and a desorption zone that desorbs the adsorbed components by applying a high-temperature desorption gas to the activated carbon after adsorption are integrated into one system via an intermediate gas seal zone. The adsorbent is contained in an endless belt-like porous case and is arranged to move cyclically between the adsorption zone and the desorption zone, and the adsorbent is contained in the chamber, and the adsorbent is arranged to move cyclically between the adsorption zone and the desorption zone. and means for circulating the desorption gas from which the components have been separated back into the desorption zone. 2. The adsorbent is fibrous activated carbon formed into a sheet of predetermined dimensions, and an endless belt is made by connecting a number of cartridges with air permeable upper and lower surfaces, in which one or several sheets of this are stacked and connected by hinges. 2. The device according to claim 1, which is configured to be driven by a sprocket system and moved on a rail that also serves as a gas seal. 3. The means for separating the components contained in the desorption gas is a condenser, and the desorption gas exiting the condenser is provided with a means for reheating it during circulation to the desorption zone. equipment. 4. Claim 3, in which heat exchange is performed between the desorption gas from the desorption zone and the desorption gas after the condensed components have been separated in the condenser, cooling the former and heating the latter. equipment. 5. The desorption zone has a relatively low-temperature desorption chamber and a relatively high-temperature desorption chamber, and the relatively low-temperature desorption gas heated by the above heat exchange first enters the low-temperature desorption chamber and once leaves there. After being heated to a relatively high temperature by a heater, the pipe is piped to enter the high-temperature desorption chamber, and the adsorbent that has adsorbed specific components that have migrated from the adsorption zone is preheated in the low-temperature desorption chamber and then enters the high-temperature desorption chamber. The patent is configured so that most of the desorption takes place there, and then the device re-enters the low-temperature desorption chamber to heat the low-temperature desorption gas to complete the desorption, while its own temperature decreases and returns to the adsorption zone. Apparatus according to claim 4. 6. The device according to claim 1, wherein the pressure in the desorption zone is kept slightly higher than that in the adsorption zone.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12409578A JPS5551418A (en) | 1978-10-11 | 1978-10-11 | Method and apparatus for continuously adsorption-desorption |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12409578A JPS5551418A (en) | 1978-10-11 | 1978-10-11 | Method and apparatus for continuously adsorption-desorption |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5551418A JPS5551418A (en) | 1980-04-15 |
| JPS6158212B2 true JPS6158212B2 (en) | 1986-12-10 |
Family
ID=14876791
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP12409578A Granted JPS5551418A (en) | 1978-10-11 | 1978-10-11 | Method and apparatus for continuously adsorption-desorption |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5551418A (en) |
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| JPS63291396A (en) * | 1987-05-25 | 1988-11-29 | Hiroshi Sakamura | Automatic illuminance control device for fluorescent lamp |
| CN109012013A (en) * | 2018-06-22 | 2018-12-18 | 佛山市墺林环保科技有限公司 | A kind of method and device of exhaust gas desorption condensing recovery |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5775121A (en) * | 1980-10-27 | 1982-05-11 | Mitsubishi Heavy Ind Ltd | Method and apparatus for treating waste gas at coating |
| US4511375A (en) * | 1984-03-29 | 1985-04-16 | Union Carbide Corporation | Process and apparatus for direct heat transfer temperature swing regeneration |
| US4650575A (en) * | 1985-07-03 | 1987-03-17 | Pall Corporation | Sorbing apparatus |
| JP2514698B2 (en) * | 1988-09-26 | 1996-07-10 | 株式会社大氣社 | Gas treatment equipment |
| JPH0332703A (en) * | 1989-06-29 | 1991-02-13 | Agency Of Ind Science & Technol | Continuous adsorption, desorption and regeneration device |
| EP0796655A1 (en) * | 1996-03-19 | 1997-09-24 | Heiyo Shoji Kabushiki Kaisha | Method of activating a material to be activated for adsorbent |
| JP5121288B2 (en) * | 2007-04-16 | 2013-01-16 | サカタインクス株式会社 | Organic solvent-based printing ink composition printing system and organic solvent-based printing ink composition used in the printing system |
| KR100966481B1 (en) * | 2008-01-29 | 2010-06-29 | 한국에너지기술연구원 | Continuous concentrating system and method of volatile organic compounds using moving-bed reactor |
| JP2009291685A (en) * | 2008-06-03 | 2009-12-17 | Ihi Corp | Device and method for recovering volatile organic compound |
| JP2014158991A (en) * | 2013-02-19 | 2014-09-04 | Morikawa Co Ltd | Desorption device of adsorbed volatile organic compound |
| CN103990354A (en) * | 2014-05-29 | 2014-08-20 | 江苏兆年涂装科技有限公司 | Waste gas concentration device |
| CN109012014A (en) * | 2018-06-22 | 2018-12-18 | 佛山市墺林环保科技有限公司 | A kind of method and device of exhaust gas active-carbon adsorption desorption condensing recovery |
-
1978
- 1978-10-11 JP JP12409578A patent/JPS5551418A/en active Granted
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63291396A (en) * | 1987-05-25 | 1988-11-29 | Hiroshi Sakamura | Automatic illuminance control device for fluorescent lamp |
| CN109012013A (en) * | 2018-06-22 | 2018-12-18 | 佛山市墺林环保科技有限公司 | A kind of method and device of exhaust gas desorption condensing recovery |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5551418A (en) | 1980-04-15 |
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